Untitled record

Full Description

Background of the sister

The invention generally relates to hydrogenation methods and to hydrogenation catalysts. More specifically, the present disclosure relates to methods for selectively hydrogenating acetylene, e.g., in front-end processes; to methods for starting

<p dir="rtl">5 A selective hydrogenation reactor, for example, in front-end processes; and hydrogenation catalysts are useful in such methods.</p>

Olefins are important monomers for the production of plastics. For example, ethylene and propylene are polymerized to form polyethylene and polypropylene, respectively. Olefins such as ethylene are derived from

<p dir="rtl">10 Propylene is typically obtained from petroleum products through thermal or catalytic cracking of hydrocarbons. However, cracking provides a crude olefin mixture that can contain acetylene, which can interfere with the postpolymerization of ethylene and propylene. It may be desirable to "clean" this process gas to convert acetylene to ethylene selectively without significant reduction of any existing olefins or acetylene.</p>

<p dir="rtl">15 acetylene itself to alkanes.</p>

There are two main reactor configurations for the selective hydrogenation of acetylene in ethylene-rich streams—called back-end (or tail-end) processes and front-end processes. In the back-end configuration, the feed stream to the selective hydrogenation reactor typically consists primarily of

<p dir="rtl">20 From C2 hydrocarbons, equivalent amounts of hydrogen with respect to acetylene are added to this feed gas stream to ensure an optimum concentration of</p>

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Hydrogen (typically 1–4% by mole) is present in the feed stream to the reactor. Carbon monoxide is usually not present in the feed stream in amounts greater than 2 ppm; in some conventional processes, carbon monoxide (CO) is added separately to the reactor inlet stream. In the forward configuration, the feed stream contains

<p dir="rtl">5 The feed to a selective hydrogenation reactor typically contains a large excess of hydrogen, e.g., 10–35 mole % hydrogen, along with carbon monoxide, acetylene, olefins and other hydrocarbons. In the forward deethanizer design, the reactor feed contains C2 and a lighter stream, while in the depropanizer</p>

<p dir="rtl">10 Front unit, the reactor feed stream contains C3 and lighter hydrocarbons. Carbon monoxide is generally present in this feed stream, with concentrations ranging from less than 100 ppm to 3000 ppm.</p>

Traditionally, the forward selective hydrogenation of acetylene in an olefin rich mixture is performed using enhanced catalysts.

<p dir="rtl">15 Optionally with palladium coating. However, the activity of the hydrogenation catalyst under process conditions must be carefully restricted to avoid thermal runaway (an uncontrolled feedback loop, where the heat generated by the exothermic hydrogenation reaction increases the catalyst temperature, which in turn increases the rate of the hydrogenation reaction, which provides more heat, etc.), which can lead to an undesirable severe reduction of ethylene to ethane and even to shutdown of the process.</p>

<p dir="rtl">20 The reactor is subject to uncontrollable high temperatures in the reactor. Conventional SPH processes are also severely limited by strict temperature control, which is maintained below a certain temperature (e.g., the escape temperature). Conventional SPH processes are limited by the gas hourly space velocity (GHSV), so that the temperature does not rise due to the exothermic hydrogenation reaction required to clean up the reactor.</p>

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Acetylene is very hot, so it does not approach the temperature that might lead to runaway heat.

.thermal runaway

Furthermore, reactors for these conventional forward selective hydrogenation processes, particularly those with a new catalyst, must be started up carefully to avoid thermal runaway.

<p dir="rtl">5 Traditionally, it is understood that the initial contact of the catalyst bed with the process gas stream (i.e., containing hydrogen, olefin and acetylene) must be carried out at a low temperature to avoid runaway. However, at such low temperatures, the reduction of acetylene is usually not complete and the acetylene concentration in the reactor stream is therefore higher than the product specifications allow. As the process gas flows, the temperature of the catalyst bed is raised.</p>

<p dir="rtl">10 The catalyst is then very slowly reduced to the desired reaction temperature at which the acetylene concentration is sufficient.</p>

Acetylene is within specifications. The temperature rise is often in the order of degrees Celsius per hour, so the start-up procedure can take more than twenty hours to provide output within specifications. During the start-up period, the stream flowing from the non-conforming reactor is often sent to ignition.

<p dir="rtl">15 In addition to strict temperature control, traditionally, during operation the reactor is precharged with carbon monoxide (CO) and pressurized with non-reactive gases before the catalyst is heated. The composition of the reactor gas mixture slowly shifts toward the process gas (i.e., containing hydrogen, acetylene, and one or more olefins). This start-up process not only poses safety concerns because a large amount of</p>

<p dir="rtl">20 of carbon monoxide (CO) on-site, but it is also expensive, due to material costs, time wasted in production, and treatment/disposal of reactor product before the reactor is operating at full capacity.</p>

US Patent No. 2013102819 relates to a catalyst composition for selective hydrogenations, e.g., for the selective hydrogenation of acetylene.

<p dir="rtl">25 acetylene in the gaseous phase, which involves a heterogeneous catalyst.</p>

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heterogeneous catalyst with a BET surface area of ​​≦9 m2/g and an ionic medium applied to the same surface. The catalyst formulation has improved properties, such as, for example, improved selectivity in favor of the desired product and better thermal stability.

US Patent No. 2005113613 reveals the process of removing alkenes.

<p dir="rtl">5 alkynes and/or diolefins selectively from a feedstock also containing olefins, the process comprising contacting the feedstock with hydrogen in the presence of a catalyst composition comprising a carrier and at least one metallic component selected from groups 8 to 10 of the periodic table of elements, wherein the catalyst composition is produced in a manner comprising: (a) impregnating the carrier with a compound consisting of at least one of said metals; (b) contacting said carrier 10 with at least one organic compound containing nitrogen; and (c) calcining the carrier.</p>

Accordingly, there is still a need for a method to selectively hydrogenate acetylene with high yields, and/or with low CO (carbon monoxide) concentrations, but without unnecessary risk of runaway heat. There is also a need for a method to start up a hydrogenation reactor that does not require pre-charging of the reactor with CO (carbon monoxide), nor inert gas pressure, and/or can be performed in a short period of time.

General description of the invention

The present inventors have discovered that the catalysts described herein have particularly useful properties that permit new methods for the selective hydrogenation of acetylene.

.acetylene 20

Accordingly, one aspect of the disclosure is a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition comprising a porous support material, palladium, and at least one ionic liquid with a process gas comprising

Ethylene, present in the process gas in an amount of at least 10 mole %;

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Acetylene, present in the process gas in an amount of at least 1 ppm; hydrogen, present in the process gas in an amount of at least 5 mole %; and

0 1 ppm to 190 ppm carbon monoxide;

Where at least 90% of the acetylene in the process gas is hydrogenated, and no more than 1% by mole of the total acetylene and ethylene present is converted

In the process gas to ethane.

Another aspect of the disclosure is a method for selectively hydrogenating acetylene.

hydrogenating acetylene

The method includes contacting a catalyst composition comprising a porous carrier, palladium, and at least one ionic liquid 10 with a process gas comprising

Ethylene, present in the process gas in an amount of at least 10 mole %;

Acetylene, present in the process gas in an amount of at least 1 ppm; hydrogen, present in the process gas in an amount of at least 5 mole %; and

600 At least 1 ppm of carbon monoxide;

<p dir="rtl">15 Where at least 90% of the acetylene in the process gas is hydrogenated,</p>

Not more than 1 mole percent of the total acetylene and ethylene in the process gas is converted to ethane.

Another aspect of the disclosure is a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition comprising a carrier

<p dir="rtl">20 Porosity, palladium, and at least one ionic medium with a process gas comprising</p>

Ethylene, present in the process gas in an amount of at least 10 mole %;

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Acetylene, present in the process gas in an amount of at least 1 ppm;

Hydrogen, present in the process gas in an amount of at least 5 mole %; and

where the process gas is in contact with the catalyst at a gas hourly space velocity (GHSV) of at least 7,100 h-1 (e.g., 7,500 h-1 to 5,40,000 h-1) depending on the total catalyst bed volume; and

Where at least 90% of the acetylene in the process gas is hydrogenated, and not more than 1% by mole of the total acetylene and ethylene in the process gas is converted to ethane.

Another aspect of the disclosure is a method for starting a selective 10 hydrogenation reactor, the reactor having one or more catalyst beds containing

Each of which has a suitable catalyst for selectively hydrogenating acetylene in a process gas comprising at least 10 mole % of ethylene, at least 1 ppm of acetylene, and at least 5 mole % of hydrogen, the method comprising

Providing each catalyst layer at not more than a first temperature, the catalyst of the catalyst layer is in contact with a first gas, the first gas being unreactive in the presence of the catalyst at the first temperature;

In the presence of the first gas, heating each catalyst layer to at least a second temperature, the second temperature being at least 10 degrees higher than the first temperature, the first gas being unreactive in the presence of the catalyst at the second temperature; and then

Changing the composition of the gas in contact with the catalyst from the first gas to the process gas stream while the catalyst bed 20 is at at least the second temperature; and

Allow the process gas to flow through the catalyst bed until the acetylene concentration at the reactor outlet is less than 1 ppm.

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In certain such embodiments, the initial temperature is in the range of 31-50°C, e.g., 3145°C, or 31-40°C. In other such embodiments, the initial temperature is in the range of 35-50°C, e.g., 35-45°C, or 35-40°C. In other such embodiments, the initial temperature is in the range of 40-50°C, e.g.,

5 40-45 degrees Celsius,

Another aspect of the disclosure is a method for starting a selective hydrogenation reactor, the reactor having one or more catalyst beds each containing a catalyst suitable for selectively hydrogenating acetylene in a process gas comprising at least 10 mole% ethylene, at least 1 ppm acetylene, and 5

<p dir="rtl">10 % by mole of hydrogen at least, the method includes;</p>

Providing the reactor with each catalyst bed having a catalyst in contact with a first gas, the first gas being unreactive in the presence of the catalyst at the first temperature, where the catalyst in the reactor is not in contact with a gas containing carbon monoxide that has a carbon monoxide concentration exceeding 100 parts per million; and

<p dir="rtl">15 Introducing the process gas flow into one or more catalyst beds, and refraining from adding carbon monoxide to the process gas.</p>

These methods may further include raising the catalyst bed temperature of each catalyst bed from no more than a first temperature to at least a second temperature (e.g., before, during or after changing the gas in contact with the catalyst from the first gas to the process gas).

<p dir="rtl">20 Another aspect of the disclosure is a method for starting a selective hydrogenation reactor.</p>

hydrogenation reactor, the reactor having one or more catalyst beds each containing a catalyst suitable for selectively hydrogenating acetylene in a process gas comprising at least 10 mole% ethylene, at least 1 ppm acetylene, and at least 5 mole% hydrogen, the method comprising

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Providing each catalyst layer at no more than a first temperature, the catalyst layer of the catalyst is in contact with the gas;

In the presence of the process gas, each catalyst layer is heated to at least a second temperature, the second temperature being at least 20 degrees higher than the first temperature, the heating of each layer is carried out

<p dir="rtl">5 Stimulated at a rate in the range of at least 3°C/h; and</p>

Allow the process gas to flow through the catalyst bed until the acetylene concentration at the reactor outlet is less than 1 ppm.

Another aspect of the disclosure is a method for starting a selective hydrogenation reactor, the reactor having one or more catalyst beds containing

<p dir="rtl">10 Each of which has a suitable catalyst for selectively hydrogenating acetylene in a process gas containing at least 10 mole % of ethylene, at least 1 ppm of acetylene,</p>

And at least 5% by mole of hydrogen, the method includes

Dry one or more layers of catalyst at a temperature of at least 50°C; then

<p dir="rtl">15 Cooling each dried catalyst layer to a first temperature in the range of 31-50°C (e.g., 3145°C, 31-40°C, 35-45°C, 35-40°C, 50-40°C, or 40-45°C), and contacting the catalyst of each catalyst with the process gas at the first temperature; then</p>

In the presence of the process gas, heating each catalyst layer to at least a second temperature, the second temperature being at least 20 degrees higher than the first temperature; and

Allow the process gas to flow through the catalyst bed until the acetylene concentration at the reactor outlet is less than 1 ppm.

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Another aspect of the disclosure is a hydrogenation catalyst composition comprising:

A porous carrier material, present in the composition in an amount within the range of 90% by weight to 99.9% by weight;

Palladium, present in the composition in an amount within the range 0.02 wt% to 0.5 wt%, or 0.03 wt% to 0.4 wt%, or 0.04 wt% to 0.3 wt%, calculated on the basis of mass

<p dir="rtl">5 racism; and</p>

One or more ionic liquids, present in the composition in a combined amount of up to 10% by weight.

Another aspect of the disclosure is a hydrogenation catalyst composition comprising:

A porous carrier material, present in the composition in an amount within the range of 90% by weight to 99.9% by weight,

Have a BET surface area of ​​not more than 10 m2/g and a pore volume of at least 0.1 mL/g;

<p dir="rtl">10 Palladium, present in the composition in an amount within the range of at least 0.02% by weight, calculated on the basis of elemental mass; and</p>

One or more ionic liquids, present in the composition in a combined amount of up to 10% by weight.

Another aspect of the disclosure is a hydrogenation catalyst composition comprising:

A porous carrier material, present in the composition in an amount within the range of 90% by weight to 99.9% by weight;

<p dir="rtl">15 Palladium, present in the composition in an amount within the range of at least 0.02% by weight, calculated on the basis of elemental mass; and</p>

One or more ionic liquids, present in the composition in a combined amount of up to 10% by weight,

Where the hydrogenation catalyst has a BET surface area of ​​not more than 10 m2/g and a pore volume of at least 0.05 mL/g.

20

These hydrogenation catalyst compositions can be usefully used in the methods described herein.

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Other aspects of the disclosure will be apparent to a person of ordinary skill in the art in light of the disclosure in this application.

Brief explanation of the drawings

Figure 1 is a set of graphs showing the concentration of acetylene 5 and ethylene in the product of a process described herein (left) and the product of a conventional process (right).

Figure 2 is a graph showing the ethylene selectivity (left y-axis) of the process described herein (middle line) and a conventional process (bottom line) through several variations in CO (carbon monoxide) concentration (top line, right y-axis).

<p dir="rtl">10 Figure 3 is a set of graphs showing the conversion of acetylene (left) and the selectivity of ethylene (right) for the various processes described in this application.</p>

Figure 4 is a set of graphs showing the conversion of acetylene (left) and the selectivity of ethylene (right) for the various processes described in this application.

Figures 5, 6, 7 and 8 are graphs of reactor temperatures for start-up experiments according to Example

<p dir="rtl">15 6.</p>

Figure 9 is a graph of the selectivity of acetylene removal with respect to carbon monoxide (CO) concentration under isothermal conditions for a catalyst as described herein and a comparable catalyst.

Detailed description:

20 The fourth difference is related to the selectively hydrogenating methods of acetylene.

C2H2(acetylene) by contacting a process gas containing acetylene with a catalyst composition comprising a porous carrier, palladium, one or more ionic liquids, and optionally

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10

15

20

catalysts such as silver, gold, zinc, tin, lead, gallium, cadmium, copper, bismuth, sodium, cesium, or potassium. The present inventors have determined that these catalysts can unexpectedly provide improved operation of hydrogenation systems by permitting selective hydrogenation of acetylene without thermal runaway under a wider variety of conditions than previously envisioned.

For example, in certain aspects of the detection, carbon monoxide (CO) may be present in the process gas, if present at all, only in a relatively small amount (e.g., in the range of 0 to 190 ppm, 0 to 175 ppm, or 0 to 150 ppm, calculated on a molar basis). This can allow operations to be conducted without adding carbon monoxide (CO) to a low-CO feed stream, simplifying the process and improving plant safety.

In other aspects, carbon monoxide (CO) may be present in the process gas in a relatively large amount (e.g., at least 600 ppm, or in a range of 600 ppm to 20,000 ppm, or 600 ppm to 10,000 ppm). This may permit the use of process gases with high CO. In various aspects, the process gas may be contacted with the catalyst composition at a relatively high gas hourly space velocity (GHSV) (e.g., at least 7,100 h-1, at least 10,000 h-1, or at least 12,500 h-1, for example in the range from 7,100 h-1 to 40,000 h-1, or in the range from 10,000 h-1 to 40,000 h-1, or in the range from 12,500 h-1 to 40,000 h-1). The present inventors have determined that the catalysts described herein can be used at unexpectedly high reaction flows without escape. In certain embodiments, the selective hydrogenation is carried out at a relatively high temperature, allowing for increased reaction rate and increased productivity. The disclosure demonstrates that these selective hydrogenation methods can advantageously provide the selective conversion of desired acetylene and the conversion of ethylene

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Relatively little ethylene (ethane; ethylene) (C2H4) without thermal runaway.

Accordingly, one aspect of the disclosure is a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition with a process gas.

<p dir="rtl">5 The catalyst composition consists of a porous carrier, palladium, and one or more ionic liquids. The gas mixture includes ethylene, present in the process gas in an amount of at least 15 mole %; acetylene, present in the process gas in an amount of at least 1 ppm; hydrogen, present in the process gas in an amount of at least 5 mole %; and 0 to 190 ppm of carbon monoxide. At least 90% is hydrogenated</p>

<p dir="rtl">10 of acetylene present in the process gas and selectively hydrogenating it without thermal runaway. Another aspect of the disclosure is a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition with a process gas. The catalyst composition includes a porous support material, palladium, and one or more ionic liquids. The gas mixture includes ethylene, present in the process gas in an amount of 15</p>

<p dir="rtl">15 % by mole; acetylene, present in the process gas in an amount of at least 1 ppm; hydrogen, present in the process gas in an amount of at least 5 % by mole; and at least 600 ppm of carbon monoxide. At least 90% of the acetylene present in the process gas is hydrogenated and the selective hydrogenation is carried out without thermal runaway. In certain embodiments, the contact is carried out at a speed of</p>

<p dir="rtl">20 Gas Hourly Space Velocity (GHSV) within the range of 2,000 h-1 to 40,000 h-1.</p>

The term “thermal runaway” describes a process in which the heat released from a catalyzed exothermic reaction (e.g., hydrogenation) increases the temperature of the catalyst, thereby accelerating the rate of the catalyzed reaction. In contrast, the amount of heat released from the accelerating reaction increases, thereby increasing the temperature of the catalyst.

<p dir="rtl">25 Catalyst temperature. A person with ordinary skill in the art will realize that, in the case of hydrogenation,</p>

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Acetylene, this thermal runaway process results in the increased formation of ethane (C2H6). Accordingly, as used herein, the term “thermal runaway” describes a process in which at least 90% of the acetylene in a process gas is hydrogenated, and not more than 1 mole percent of the total acetylene 5 and ethylene in the process gas is converted to ethane. That is, of the acetylene present in the process gas input to the method, at least 90% is hydrogenated. Ethylene and acetylene are typical components of process gases that can be excessively reduced to form ethane; the present inventors note that the amount of this undesirable excessive reduction can be reduced by the use of catalysts and methods in this application. Thus, “not more than 1 mole percent of the total acetylene and ethylene in the process gas is converted to ethane” means that the amount of ethane output from the process does not increase by more than 1 mole percent based on the total reactor product gas content compared to the input process gas. For example, if the input process gas stream contains 20 mole percent ethane, the output stream contains not more than 21 mole percent ethane.

<p dir="rtl">15 As used herein, selectivity is defined as the fraction of acetylene converted to ethylene, i.e., (ethylene gain)/(acetylene loss).</p>

Another aspect of the disclosure is a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition with a process gas at a gas hourly space velocity (GHSV) of at least 20 7,100 h-1 (e.g., in the range 7,500 h-1 to 40,000 h-1).

<p dir="rtl">1(. GAS HOURLY SPACE VELOCITY) values ​​are specified by reference to the size of the catalyst layer(s). The catalyst composition includes a porous carrier, palladium, and one or more ionic liquids. The process gas includes ethylene, present in the process gas in an amount of at least 15 mole %; acetylene, present in the process gas in an amount of at least 1 ppm; and hydrogen, present in</p>

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Process gas in an amount of at least 2 mole %. At least 90% of the acetylene in the process gas is hydrogenated, and the selective hydrogenation is performed without thermal runaway (i.e., not more than 1 mole % of the total acetylene and ethylene in the process gas is converted to ethane). 5 The present inventors have determined that the high selectivity of the catalysts described herein can allow operation at unexpectedly high vacuum capacity. In certain embodiments such as these, the process gas contains up to 20,000 ppm of carbon monoxide.

Process gas contact can be performed using a variety of equipment familiar to one of ordinary skill in the art. For example, the catalyst composition may be contained in a single layer within a vessel.

<p dir="rtl">10 A reactor or its division between a set of layers within the reactor. The reaction system may also contain one or more reaction vessels in series. The feed stream into the reaction zone may flow vertically upward, downward through the catalyst bed in a typical plug flow reactor, or horizontally through the catalyst bed in a radial flow reactor. The reaction vessels may be adiabatic reactors with internal coolers, or cooled reactors, for example tubular isothermal reactors where</p>

<p dir="rtl">15 The catalyst is in the tubes or the cooling medium is in the tubes. In some embodiments, at least 90% of the acetylene in the process gas can be hydrogenated by contact with a catalyst composition contained in a single layer.</p>

In other embodiments, at least 90% of the acetylene in the process gas may be hydrogenated by contact with a catalyst composition divided between a plurality of layers. Whereas the gas may be provided

<p dir="rtl">20 Treatment as a single stream, or it can be divided into multiple streams (e.g., a hydrogen and a hydrocarbon stream) that are combined in a reactor.</p>

The present inventors have specified that, advantageously, the methods as otherwise described herein can provide advantageous performance in, for example, otherwise conventional olefin processing systems. For example, the methods as otherwise described herein can be performed to selectively hydrogenate

<p dir="rtl">25 Acetylene contained in a crude olefin stream produced by cracking (i.e., feed stream</p>

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(a hydrocarbon feed gas), or the system overhead stream to separate C3 hydrocarbons (i.e., a depropanizer) or C2 hydrocarbons (i.e., a deethanizer) from the olefin stream. In another example, the methods as otherwise described herein may be performed to selectively hydrogenate acetylene contained in the refinery exhaust gas stream. Accordingly, in various embodiments as

<p dir="rtl">5 Otherwise described in this application, the process gas is provided from a cracker flow stream, from an overflow stream from a depropanizer, from an overflow stream from a deethanizer, or from a refinery exhaust gas stream.</p>

In certain embodiments of the methods as otherwise described herein, the selective hydrogenation is carried out at a temperature within the range of 20°C to 140°C. In embodiments

<p dir="rtl">10 For a certain desired purpose, the selective hydrogenation is performed at a temperature within the range of 40°C to 100°C, e.g., 40°C to 90°C, 50°C to 100°C, or 50°C to 90°C. However, the processes can be performed at a variety of temperatures. For example, in certain embodiments such as these, the selective hydrogenation is performed at a temperature within the range of 20°C to 130°C, e.g., in the range of 20°C</p>

<p dir="rtl">15 120°C to 120°C, 20°C to 110°C, 20°C to 100°C, or 20°C to 90°C. In such other embodiments, the selective hydrogenation is carried out at a temperature within the range of 40°C to 140°C, e.g., 40°C to 130°C, 40°C to 120°C, or 40°C to 110°C. In such other embodiments, the selective hydrogenation is carried out at a temperature within the range of 40°C to 140°C, e.g., 40°C to 130°C, 40°C to 120°C, or 40°C to 110°C.</p>

<p dir="rtl">20 Temperature within the range of 50°C to 140°C, e.g. 50°C to 130°C</p>

°C, or 50°C to 120°C, or 50°C to 110°C. In such other embodiments, the selective hydrogenation is carried out at a temperature within the range of 60°C to 140°C, e.g., 60°C to 130°C, or 60°C to 120°C, or 60°C to 110°C, or 60°C to

25 100°C, or 60°C to 90°C.

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Helpfully, the present inventors have specified that the process gas according to the methods as otherwise described herein may include carbon monoxide (CO) in an amount within a relatively wide range. For example, the present inventors have noted that prior art processes typically include a certain amount of carbon monoxide in the process feed stream, in order to add carbon monoxide to a process feed stream that does not contain sufficient carbon monoxide. The purpose of the carbon monoxide is to mediate the activity of the catalyst, so that the process does not proceed and produce more ethane than desired. It was understood that the presence of conventional catalysts with low selectivity for acetylene hydrogenation, especially at lower carbon monoxide concentrations, and the addition of carbon monoxide was desirable to maintain a relatively low amount of ethane.

ethane in the process product. In contrast, the present inventors have determined that the catalysts described herein can provide high selectivity without escape even at low CO concentrations. Accordingly, in certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount up to 190 ppm, e.g., 15 within the range of 1 ppm to 190 ppm, e.g., within the range of 5 ppm to 190 ppm, 10 ppm to 190 ppm, 25 ppm to 190 ppm, 50 ppm to 190 ppm, or 100 ppm to 190 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount of 20 to 180 parts per million, e.g., within the range of 1 part per million to 180 parts per million,

For example, in the range of 5 ppm to 180 ppm, 10 ppm to 180 ppm, 25 ppm to 180 ppm, 50 ppm to 180 ppm, or 100 ppm to 180 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) 25 MONOXIDE is present in the process gas in an amount up to 170 ppm, e.g., within the range of 1 ppm to 170 ppm, e.g., within the range of 5 ppm to 170

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parts per million, or 10 parts per million to 170 parts per million, or 25 parts per million to 170 parts per million, or 50 parts per million to 170 parts per million, or 100 parts per million to 170 parts per million. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount up to 160 parts per million.

<p dir="rtl">5 In the range of 1 ppm to 160 ppm, for example, in the range of 5 ppm to 160 ppm, 10 ppm to 160 ppm, 25 ppm to 160 ppm, 50 ppm to 160 ppm, or 100 ppm to 160 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas</p>

<p dir="rtl">10 In an amount up to 150 ppm, for example, within the range of 1 ppm to 150 ppm, for example, within the range of 5 ppm to 150 ppm, or 10 ppm to 150 ppm, or 25 ppm to 150 ppm, or 50 ppm to 150 ppm, or 100 ppm to 150 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO)</p>

<p dir="rtl">15 MONOXIDE in the process gas in an amount up to 140 ppm, for example, within the range of 1 ppm to 140 ppm, for example, within the range of 5 ppm to 140 ppm, or 10 ppm to 140 ppm, or 25 ppm to 140 ppm, or 50 ppm to 140 ppm, or 100 ppm to 140 ppm. In certain embodiments of the methods as otherwise described herein, the first</p>

<p dir="rtl">20 CARBON MONOXIDE) in the process gas in an amount up to 130 ppm, for example, within the range of 1 ppm to 130 ppm, for example, within the range of 5 ppm to 130 ppm, or 10 ppm to 130 ppm, or 25 ppm to 130 ppm, or 50 ppm to 130 ppm, or 100 ppm to 130 ppm. In certain embodiments of the methods as described otherwise</p>

<p dir="rtl">25 In this application, carbon monoxide (CO) is present in the process gas in an amount of up to 120 ppm, i.e., within the range of 1 ppm to 120 ppm.</p>

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In the range of 5 ppm to 120 ppm, 10 ppm to 120 ppm, 25 ppm to 120 ppm, or 50 ppm to 120 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount up to 5 110 ppm, for example, in the range of 1 ppm to 110 ppm, for example.

For example, in the range of 5 ppm to 110 ppm, 10 ppm to 110 ppm, 25 ppm to 110 ppm, or 50 ppm to 110 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount up to 100 ppm.

<p dir="rtl">10 In the range of 1 ppm to 100 ppm, for example, in the range of 5 ppm to 100 ppm, 10 ppm to 100 ppm, 25 ppm to 100 ppm, or 50 ppm to 100 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount up to 90 ppm, for example,</p>

<p dir="rtl">15 Within the range of 1 ppm to 90 ppm, for example, within the range of 5 ppm to 90 ppm, or 10 ppm to 90 ppm, or 25 ppm to 90 ppm, or 50 ppm to 90 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount up to 80 ppm, for example, within the range of 1</p>

<p dir="rtl">20 ppm to 80 ppm, for example, in the range of 5 ppm to 80 ppm, 10 ppm to 80 ppm, 25 ppm to 80 ppm, or 50 ppm to 80 ppm. In certain embodiments of the methods as otherwise described herein, carbon monoxide (CO) is present in the process gas in an amount up to 50 ppm, for example, in the range of 1 ppm to 50 ppm.</p>

<p dir="rtl">25 In million, for example, in the range of 5 ppm to 50 ppm, 10 ppm to 50 ppm, or 25 ppm to 50 ppm. In certain models of</p>

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Methods as otherwise described in this application, essentially no carbon monoxide (CO) is present in the process gas.

Significantly, in certain embodiments of the methods as otherwise described herein, carbon monoxide is not added to a feed gas stream to provide the process gas. That is, 5 unlike many conventional methods, in certain embodiments as otherwise described herein

The application does not maintain a sufficiently low CO (carbon monoxide) concentration in the process gas to maintain a sufficiently low heat output due to the hydrogenation of ethylene. Instead, the catalyst described herein is highly selective for the hydrogenation of acetylene to ethylene, even at low CO concentrations, and thus there is little thermal runaway due to the reduction of ethylene at

This low CO2 emissions are very common.

The present inventors note that a process gas containing high carbon monoxide (CO) can result in variations in the pre-process step, and that continuous hydrogenation performance throughout and/or after such variation would also be desirable. The present inventors 15 note that the catalysts described herein can provide continuous, non-fouling production of downstream gases at CO levels as high as 20,000 ppm, even at temperatures significantly higher than those normally required for CO concentrations (i.e., comparable to the temperatures required for acetylene cleanup at low CO levels). Remarkably, as described in Example 7 below, the catalysts described herein can have relatively constant acetylene selectivity even at high oxidation concentrations.

CARBON MONOXIDE (CO) is higher. In certain embodiments as otherwise described herein, CO is present in the process gas in an amount of at least 600 ppm (e.g., at least 800 ppm, at least 1,000 ppm, at least 1,500 ppm, or at least 2,000 ppm). For example, in certain embodiments as described

<p dir="rtl">25 Otherwise in this application, carbon monoxide (CO) is present in the gas.</p>

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Treatment in an amount within the range of 600 ppm to 20,000 ppm. For example, in certain embodiments such as these, carbon monoxide (CO) is present in the treatment gas in an amount within the range of 600 ppm to 15,000 ppm, or 600 ppm to 10,000 ppm, or 600 ppm to 5,000 ppm, or

<p dir="rtl">5 600 ppm to 2,500 ppm, or 600 ppm to 1,500 ppm,</p>

or 700 ppm to 1,200 ppm, or 800 ppm to 1,200 ppm, or 900 ppm to 1,200 ppm, or 700 ppm to 1,000 ppm, or 800 ppm to 1,100 ppm. In such other embodiments, carbon monoxide (CO) is present in the process gas in an amount in the range of 800 ppm

<p dir="rtl">10 ppm to 20,000 ppm, or 800 ppm to 15,000 ppm, or 800 ppm to 10,000 ppm, or 800 ppm to 5,000 ppm, or 800 ppm to 2,500 ppm, or 800 ppm to 1,500 ppm. In such other embodiments, carbon monoxide (CO) is present in the process gas in an amount in the range of 1,000 ppm to 20,000 ppm, or 1,000</p>

<p dir="rtl">15 ppm to 15,000 ppm, or 1,000 ppm to 10,000 ppm, or 1,000 ppm to 5,000 ppm, or 1,000 ppm to 2,500 ppm. In other such embodiments, the CO (Carbon) MONOXIDE is present in the process gas in an amount in the range of 1,500 ppm to 20,000 ppm, or 1,500 ppm to 15,000 ppm, or 1,500 ppm to</p>

<p dir="rtl">20 10,000 ppm, or 1,500 ppm to 5,000 ppm. In such models</p>

Other, carbon monoxide (CO) is present in the process gas in an amount in the range of 2,000 ppm to 20,000 ppm, 2,000 ppm to 15,000 ppm, 2,000 ppm to 10,000 ppm, or 2,000 ppm to 5,000 ppm.

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However, in other embodiments, the process gas may have a different CO concentration. For example, in certain embodiments (e.g., when the gas hourly space velocity (GHSV) is at least 7,500 h-1, at least 10,000 h-1, at least 15,000 h-1 or at least

<p dir="rtl">5 20,000 hours-1(, the concentration of carbon monoxide (CO) of the gas reaches</p>

Processing to 1,200 ppm, for example, up to 1,000 ppm, up to 500 ppm, in the range of 10 ppm to 1,200 ppm, in the range of 10 ppm to 500 ppm, in the range of 50 ppm to 1,200 ppm, in the range of 50 ppm to 500 ppm, in the range of 100

<p dir="rtl">10 1 ppm to 1,200 ppm, or in the range of 100 ppm to 500 ppm.</p>

Helpfully, the present inventors have specified that the process gas according to the methods as otherwise described herein can come into contact with the catalyst composition at a relatively high rate (e.g., at least 7,100 h-1, or within the range of 7,500 h-1 to 40,000 h-1), which significantly increases the

<p dir="rtl">15 Desirable productivity. The present inventors have also specified that as a result of the high selectivity of the catalysts described herein, the methods described herein can be performed at high productivity, while retaining selectivity and without causing runaway. Accordingly, the methods described herein can be performed in a selective hydrogenation reactor (e.g., including a single-layer catalyst, or a plurality of catalyst layers) of relatively small size (i.e., compared to processes</p>

<p dir="rtl">20 Conventional to achieve the same overall product formation rate. Accordingly, in certain embodiments as otherwise described herein, the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 7,100 h-1, e.g., within the range of 7,100 h-1 to 40,000 h-1, or 7,100 h-1 to 30,000 h-1, or 7,100 h-1 to 20,000 h-1. In certain embodiments as otherwise described herein, the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 7,100 h-1, e.g., within the range of 7,100 h-1 to 40,000 h-1, or 7,100 h-1 to 30,000 h-1, or 7,100 h-1 to 20,000 h-1.</p>

<p dir="rtl">25 Otherwise described herein, the process gas is brought into contact with the catalyst at a gas vacuum velocity</p>

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7,500 HOURS-1 ON (GHSV) GAS HOURLY SPACE VELOCITY

At least, for example, within the range of 7,500 h-1 to 40,000 h-1, or 7,500 h-1 to 30,000 h-1, or 7,500 h-1 to 20,000 h-1. In certain embodiments as otherwise described herein, the process gas is contacted with the catalyst at a gas vacuum velocity

10,000 HOURS-1 ON (GHSV) GAS HOURLY SPACE VELOCITY 5 PER HOUR

At least, for example, within the range of 10,000 h-1 to 40,000 h-1, or 10,000 h-1 to 30,000 h-1, or 10,000 h-1 to 20,000 h-1. In certain embodiments as otherwise described herein, the process gas is contacted with the catalyst at a vacuum velocity

<p>-15,000 GAS HOURLY SPACE VELOCITY (GHSV)</p>

<p dir="rtl">10 At least 1, for example, within the range of 15,000 hours-1 to 40,000 hours-1, or 15,000</p>

1 to 30,000 hours-1, or 15,000 hours-1 to 20,000 hours-1. In certain embodiments as otherwise described herein, the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 20,000 hours-1, e.g., within the range of 20,000 hours-1 to 40,000 hours-1, or

<p dir="rtl">15 20,000 h-1 to 30,000 h-1. The empty gas velocity values ​​are specified per hour.</p>

GHSV (GAS HOURLY SPACE VELOCITY) refers to the total volume of the catalyst layer(s).

As noted above, the processes described in this application are carried out so that at least 90% of the acetylene in the process gas is hydrogenated (i.e., the acetylene conversion is

<p dir="rtl">20 (90% acetylene at least). For example, in certain embodiments of the methods as described</p>

Otherwise in this application, at least 92.5%, at least 95% by mole, at least 96%, at least 97%, at least 97.5%, at least 98%, at least 98.5%, or at least 99% of the acetylene in the process gas is hydrogenated. In certain embodiments of the methods as otherwise described in this application, all of the acetylene is hydrogenated

<p dir="rtl">25 Acetylene is mainly present in the process gas.</p>

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As noted above, in various aspects, the methods as otherwise described herein may be carried out without thermal runaway, i.e., not more than 1 mole percent of the total acetylene and ethylene present in the process gas is converted to ethane. For example, in certain embodiments of the methods as otherwise described herein

<p dir="rtl">5 Request, not more than 0.9 mol %, not more than 0.8 mol %, not more than 0.7 mol %, not more than 0.6 mol %, or not more than 0.5 mol % of the total acetylene and ethylene in the process gas is converted to ethane (i.e., the amount of ethane output from the process is not more than 0.8 mol %, 0.7 mol %, 0.6 mol %, or 0.5 mol % based on the total content of the process gas compared to the input process gas).</p>

<p dir="rtl">10 For example, in certain embodiments of the methods as otherwise described herein, not more than 0.2 mole percent, e.g., not more than 0.1 mole percent, or not more than 0.05 mole percent, of the total acetylene and ethylene present in the process gas is converted to ethane. In certain embodiments of the methods as otherwise described herein, substantially none of the total acetylene and ethylene present in the process gas is converted to ethane.</p>

<p dir="rtl">15 Processing to ethane.</p>

But otherwise, the amount of ethane in the product selectively hydrogenated according to the methods as otherwise described herein may include an amount of ethane not more than 1 mole percent more than the amount of ethane in the process gas (i.e., before contact with a catalyst composition as otherwise described herein). For example, in certain embodiments, the amount of ethane 20 in the product selectively hydrogenated according to the method as otherwise described herein is not more than 0.9 mole % more, or not more than 0.8 mole % more, or not more than 0.7 mole % more, or not more than 0.6 mole % more, or not more than 0.5 mole % more than the amount of ethane in the process gas. In certain embodiments, the amount of ethane in the product selectively hydrogenated according to the method as otherwise described herein is not more than 0.2 mole % more, e.g., not more than 0.1 mole %

<p dir="rtl">25 More than, or not more than 0.05% by mole of the amount of ethane in the process gas. In models</p>

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Certainly, the amount of ethane in the product selectively hydrogenated according to the method as otherwise described herein is essentially the same as the amount of ethane in the process gas.

As described above, a wide variety of process gases can be processed using the selective hydrogenation methods described herein. For example, in certain embodiments of the methods as

<p dir="rtl">5 As otherwise described herein, ethylene is present in the process gas in an amount of at least 15 mole %. For example, in certain embodiments such as these, ethylene is present in the process gas in an amount in the range of 15 mole % to 70 mole %, or 15 mole % to 60 mole %, or 15 mole % to 50 mole %. In certain embodiments as otherwise described herein, ethylene is present in the process gas in an amount of at least 20 mole %, e.g., in the range</p>

<p dir="rtl">10 20% by mole to 70% by mole, or 20% by mole to 60% by mole, or 20% by mole to 50% by mole. In certain embodiments as otherwise described herein, ethylene is present in the process gas in an amount of at least 30% by mole, e.g., in the range of 30% by mole to 70% by mole, or 30% by mole to 60% by mole, or 30% by mole to 50% by mole.</p>

<p dir="rtl">15 Acetylene may be present in the process gas composition in a variety of quantities, depending on the specific source of the process gas. In certain embodiments of the methods as otherwise described herein, acetylene is present in the process gas in an amount of at least 10 ppm, at least 50 ppm, at least 100 ppm, or at least 500 ppm, e.g., in an amount in the range of 10 ppm to 2 mole percent, or 10 ppm</p>

<p dir="rtl">20 To 1% mole, or 10 parts per million to 0.5% mole, or 50 parts per million to 2% mole, or 50 parts per million to 1% mole, or 50 parts per million to 0.5% mole, or 100 parts per million to 2% mole, or 100 parts per million to 1% mole, or 100 parts per million to 0.5% mole, or 500 parts per million to 2% mole, or 500 parts per million to 1% mole, or 500 parts per million to 0.5% mole. In certain embodiments of the methods as otherwise described</p>

<p dir="rtl">25 In this application, acetylene is present in the process gas at an amount of 0.1 mol %.</p>

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Less than, for example, 0.5% per mole or less than 1% per mole, for example, in the range 0.1% per mole to 2% per mole, or 0.5% per mole to 2% per mole, or 1% per mole to 2% per mole, or 0.1% per mole to 1.5% per mole, or 0.5% per mole to 1.5% per mole, or 1% per mole to 1.5% per mole, or 0.1% per mole to 1% per mole, or 0.5% per mole to 1% per mole.

<p dir="rtl">5 Hydrogen can be supplied in the process gas at a variety of concentrations. A person of ordinary skill in the art will select an amount of hydrogen that will provide the necessary buffer for acetylene, and, for example, to provide the desired amount of hydrogen for the subsequent processing step. In certain embodiments as otherwise described herein, hydrogen is present in the process gas in an amount of at least 5 mole %, at least 6 mole % over 10, at least 7 mole %, at least 8 mole %, at least 9 mole %, or at least 10 mole %, for example, in the range of 5 mole % to 50 mole %, or 5 mole % to 35 mole %, or 5 mole % to 20 mole %, or 5 mole % to 15 mole %, or 8 mole % to 50 mole %, or 8 mole % to 35 mole %, or 8 mole % to 20 mole %, or 8 mole % to 15 mole %, or 10 % per mole to 50% per mole, or 10% per mole to 35% per mole</p>

<p dir="rtl">15 % per mole, or 10% per mole to 20% per mole, or 10% per mole to 15% per mole.</p>

A person of ordinary skill in the art will recognize that other components may be present in the process gas according to the methods as otherwise described herein. For example, the process gas may include one or more components typically found in a crude olefin stream produced by cracking such as, for example, C1 components (e.g., including methane, ole

<p dir="rtl">20 Carbon monoxide, carbon dioxide), C2 components (e.g., including ethylene, ethane, and acetylene), C3 components (e.g., including propane, propylene, propadiene, and methyl acetylene), and C4 components (e.g., including 1,3-butadiene). However, in certain embodiments, the process gas will not contain more than 10 mole %</p>

<p dir="rtl">25 (eg, more than 5% by mole, more than 2% by mole or more than 1% by mole) of the compounds</p>

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containing carbon other than C1 components (e.g., methane, carbon monoxide, and carbon dioxide), C2 components (e.g., ethylene, ethane, and acetylene), and C3 components (e.g., propylene, propane, methyl acetylene, and propadiene).

<p dir="rtl">5 In certain embodiments, the process gas will not contain more than 20 mole % (e.g., more than 15 mole %, more than 10 mole % or more than 5 mole %) of carbon-containing compounds other than ethylene, ethane, acetylene, carbon monoxide and carbon dioxide. In certain embodiments, the process gas will not contain more than 5 mole % (e.g., more than 2 mole %) of carbon-containing compounds other than ethylene, ethane, acetylene, carbon monoxide and carbon dioxide.</p>

<p dir="rtl">10 Containing carbon other than ethylene, ethane, acetylene, carbon monoxide and carbon dioxide.</p>

Different gas streams can be combined to provide process gas. For example, a gas stream containing hydrogen can be added to another gas stream to provide process gas. Gas streams can also be combined in the reactor to provide process gas that is a combination of the input gas streams.

<p dir="rtl">15 As noted above, in various aspects, the methods of disclosure include contacting a catalyst composition with a process gas. Accordingly, another aspect of the disclosure is a catalyst composition comprising a porous carrier, palladium, and one or more ionic liquids. In certain embodiments as otherwise described herein, the catalyst composition comprises a porous carrier selected from alumina, silica, titania, and any combination thereof. In certain such embodiments, the alumina</p>

<p dir="rtl">20 alumina, silica, titania, and any mixture thereof in the catalyst composition in a total amount within the range of 90 wt% to 99.9 wt%, calculated as oxide on a calcined basis. For example, in certain embodiments as otherwise described herein, the catalyst composition includes a porous support material selected from alumina, silica, titania, and any mixture thereof, present in the catalyst composition in an amount within the range of 92.5 wt% to 99</p>

<p dir="rtl">25 %by weight, or 95%by weight to 99.9%by weight, or 97.5%by weight to 99.9%by weight. In</p>

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In certain embodiments, the porous carrier material is a mixture of alumina and silica. In other embodiments, the porous carrier material is alumina, e.g., alpha-alumina.

As used herein, the term “oxide,” including, for example, “mixed oxide,” “alumina,” “silica,” etc., includes oxides in all crystalline forms and phases.

For example, "alumina" includes aluminium oxide (Al2O3), Al2Ox where x is in the range 1 to 3, etc. Unless otherwise stated, regardless of the actual stoichiometric quantity of oxide, oxides are calculated as the most stable oxide for purposes of determining the weight percentage. For example, someone with ordinary skill 10 in the art will realize that it is still possible to account for non-stoichiometric aluminium oxide, or even another form of aluminium, as aluminium oxide (Al2O3). Furthermore, unless otherwise noted, compositions are described as calcined.

In certain embodiments as otherwise described herein, the BET surface area of ​​the porous carrier material falls within the range of 2 m2/g to 10 m2/g. A person with 15 ordinary skill in the art will recognize that the “BET surface area” of a particular material refers to the specific surface area

For a particular material, and is determined by the standard test procedure ASTM D3663 (“Standard Test Method for Surface Area of ​​Catalysts and Catalyst Support Materials”). For example, in certain embodiments as otherwise described herein, the BET surface area of ​​the porous support material falls within the range of 2 m2/g to 9 m2/g, 2 m2/g to 8 m2/g, 2 m2/g to 7 m2/g, 20 2 m2/g to 6 m2/g, 2 m2/g to 5 m2/g, 3 m2/g to 10 m2/g, or 4 m2/g

To 10 m2/g, or 5 m2/g to 10 m2/g, or 6 m2/g to 10 m2/g, or 2 m2/g to 6 m2/g, or 3 m2/g to 7 m2/g, or 4 m2/g to 8 m2/g, or 5 m2/g to 9 m2/g. BET surface areas not exceeding 10 m2/g can be provided by calcining the carrier material to a relatively high degree.

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In certain embodiments as otherwise described herein, the pore size (determined using mercury infiltration porosity in accordance with ASTM D4284) of the porous carrier is at least 0.10 mL/g, e.g., within the range of 0.10 mL/g to 1.0 mL/g. For example, in certain embodiments as otherwise described herein, the pore size of the porous carrier is

<p dir="rtl">5 (determined using mercury infiltration porosity according to ASTM D4284) within the range of 0.10 mL/g to 0.80 mL/g, 0.20 mL/g to 0.80 mL/g, 0.30 mL/g to 0.80 mL/g, 0.20 mL/g to 0.70 mL/g, or 0.30 mL/g to 0.70 mL/g.</p>

A metal-impregnated porous carrier (i.e., including the porous carrier, palladium, and any additives present, but not the ionic liquid) can similarly have a surface area of

Relatively high, e.g., at least 0.10 mL/g (determined using mercury infiltration porosity in accordance with ASTM D4284). For example, in certain embodiments as otherwise described herein, the metal-impregnated porous carrier material has a pore volume of at least 0.15 mL/g, at least 0.20 mL/g, or up to 0.25 mL/g. In various embodiments as

<p dir="rtl">15 Otherwise described herein, the metal-impregnated porous carrier material has a pore volume in the range of 0.10 mL/g to 1.0 mL/g, e.g., 0.10 mL/g to 0.80 mL/g, 0.10 to 0.60 mL/g, 0.10 to 0.40 mL/g, or 0.10 to 0.30 mL/g.</p>

In other embodiments as otherwise described herein, the porous carrier material has

<p dir="rtl">20 The mineral impregnated porous carrier has a pore volume in the range of 0.15 mL/g to 1.0 mL/g, e.g., 0.15 mL/g to 0.80 mL/g, or 0.15 to 0.60 mL/g, or 0.15 to 0.40 mL/g, or 0.15 to 0.30 mL/g. In other embodiments as otherwise described herein, the mineral impregnated porous carrier has a pore volume in the range of 0.20 mL/g to 1.0 mL/g, e.g., 0.20 mL/g to 0.80 mL/g, or 0.20 to</p>

<p dir="rtl">25 0.60 mL/g, or 0.20 to 0.40 mL/g, or 0.20 to 0.35 mL/g. In</p>

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Other embodiments As otherwise described herein, the metal-impregnated porous carrier material has a pore size in the range of 0.25 mL/g to 1.0 mL/g, e.g., 0.25 mL/g to 0.80 mL/g, 0.25 to 0.60 mL/g, 0.25 to 0.40 mL/g, or 0.20 to 0.35 mL/g.

<p dir="rtl">5 The present inventors have identified a particular advantage when the metal-impregnated porous carrier material also has a relatively low BET surface area (i.e., not more than 10 m2/g, or a more specific range described above) combined with a high pore volume. Notably, in certain embodiments as otherwise described herein, the porous carrier material has a relatively low BET surface area (i.e., not more than 10 m2/g, or a more specific range described above) but a relatively high pore volume (i.e., an excess of 10 0.10 mL/g, e.g., within the range of 0.10 mL/g to 1.0 mL/g or a range</p>

More specifically described above. This can allow the material, after impregnation with ionic liquid as described herein, to retain some pore volume even in the presence of ionic liquid.

For example, in certain embodiments as otherwise described herein, the catalyst composition (i.e., including the porous carrier material, palladium and any present enhancers, 15 and the ionic liquid) itself has a relatively high pore volume (determined using a mercury infiltration porosity in accordance with ASTM D4284 of at least 0.05 mL/g). In certain embodiments as otherwise described herein, the catalyst composition has a pore volume of at least 0.10 mL/g, at least 0.15 mL/g, or up to 0.20 mL/g. In various embodiments as otherwise described herein, the catalyst composition has a pore size in the range of 0.05 mL/g to 1.0 20 mL/g, e.g., 0.05 mL/g to 0.80 mL/g, or 0.05 to 0.60 mL/g,

or 0.05 to 0.40 mL/g, or 0.05 to 0.30 mL/g. In other embodiments as otherwise described herein, the catalyst composition has a pore size in the range of 0.10 mL/g to 1.0 mL/g, e.g., 0.10 mL/g to 0.80 mL/g, or 0.10 to 0.60 mL/g, or 0.10 to 0.40 mL/g, or 0.10 to 0.30 mL/g. In other embodiments as otherwise described herein, the catalyst composition has a pore size in

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The range is from 0.10 mL/g to 1.0 mL/g, e.g., 0.10 mL/g to 0.80 mL/g, or 0.10 to 0.60 mL/g, or 0.10 to 0.40 mL/g, or 0.10 to 0.30 mL/g. In other embodiments as otherwise described herein, the catalyst composition has a pore size in the range from 0.15 mL/g to 1.0 mL/g, e.g., 0.15 mL/g.

<p dir="rtl">5 1 to 0.80 ml/g, 0.15 to 0.60 ml/g, 0.15 to 0.40 ml/g, or 0.15 to 0.30 ml/g. In other embodiments as otherwise described herein, the catalyst composition has a pore size in the range of 0.20 ml/g to 1.0 ml/g, e.g., 0.20 ml/g to 0.80 ml/g, 0.20 to 0.60 ml/g, 0.20 to 0.40 ml/g, or 0.20 to 0.35 ml/g. These materials can be provided using</p>

<p dir="rtl">10 A relatively low amount of ionic liquid, for example, up to 4 wt% or up to 3 wt%, depending on the pore size of the carrier material.</p>

In certain embodiments as otherwise described herein, the catalyst composition includes palladium in an amount of at least 0.02 wt % (i.e., calculated on an elemental mass basis). For example, in certain such embodiments, the catalyst composition includes palladium in an amount of

<p dir="rtl">15 At least 0.03 wt%, at least 0.04 wt%, at least 0.05 wt%, at least 0.06 wt%, at least 0.07 wt%, at least 0.08 wt%, at least 0.09 wt%, at least 0.1 wt%, at least 0.11 wt%, at least 0.12 wt%, at least 0.13 wt%, at least 0.14 wt%, or at least 0.15 wt%. In certain such embodiments, the catalyst composition comprises palladium</p>

<p dir="rtl">20 In an amount of not more than 0.5 wt% (e.g., more than 0.4 wt%, not more than 0.3 wt%, or not more than 0.2 wt%). For example, in certain embodiments as otherwise described herein, the catalyst composition comprises palladium in an amount within the range of 0.02 wt% to 0.5 wt%, 0.02 wt% to 0.45 wt%, 0.03 wt% to 0.4 wt%, 0.03 wt% to 0.35 wt%, or 0.04 wt% to</p>

25 0.3% by weight, or 0.04% by weight to 0.25% by weight.

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In certain embodiments as otherwise described herein, the palladium is placed on the surface of the carrier material, in a so-called shell catalyst configuration. The “surface” material has a significantly higher concentration (e.g., 100% higher) on the surface of the material (including an internal pore surface) than on the interior of the material. A person of ordinary skill in the art 5 will also recognize that the “surface” of the composition consists not only of the outer surface of the atoms of the composition, but also includes a surface layer at the outer portion of the composition. For example, the palladium-containing coating on the carrier material may, in certain embodiments, have a thickness of up to 1 mm. The coating thickness, in certain embodiments as otherwise described herein, may be in the range of 100-800 μm.

<p dir="rtl">10 In certain embodiments as otherwise described herein, the catalyst composition further includes at least one promoter selected from silver, gold, zinc, tin, lead, gallium, cadmium, copper, bismuth, sodium, cesium, or potassium. For example, in certain such embodiments, the catalyst composition includes a silver promoter. In such other embodiments, the catalyst composition includes a gold or zinc promoter. In certain embodiments as otherwise described herein, the promoter</p>

<p dir="rtl">15 At least one (e.g., silver) in the catalyst composition in a total amount of at least 0.02 wt % (i.e., calculated on an elemental mass basis), or at least 0.04 wt %, or at least 0.06 wt %, or at least 0.08 wt %, or at least 0.1 wt % or at least 0.12 wt %, or at least 0.14 wt %, or at least 0.16 wt %, or at least 0.18 wt %, or at least 0.2 wt %, or at least 0.22 wt %, or at least 0.24 wt %</p>

<p dir="rtl">20 At least, or at least 0.26 wt%, or at least 0.28 wt%, or at least 0.3 wt%. In certain such embodiments, the catalyst composition comprises at least one promoter in a total amount of not more than 0.6 wt% (e.g., not more than 0.45 wt%, or not more than 0.3 wt%).</p>

In certain embodiments as otherwise described herein, at least one promoter (e.g., silver) is located in addition to palladium in a shell layer. In certain embodiments, the mass ratio of

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Palladium metal to the enhancer within the range of 1:5 to 3:1, for example, within the range of 1:4 to 2:1, or within the range of 1:3 to 1:1.

In certain embodiments as otherwise described herein, the catalyst composition includes at least one ionic liquid in a total amount of up to 10 wt%. For example, in embodiments

<p dir="rtl">5 Specifically as otherwise described herein, the catalyst composition comprises at least one ionic liquid in a total amount within the range of 0.01 wt% to 10 wt%, e.g., 0.01 wt% to 8 wt%, 0.01 wt% to 6 wt%, 0.01 wt% to 4 wt%, 0.01 wt% to 3 wt%, 0.01 wt% to 2 wt%, or 0.01 wt% to</p>

<p dir="rtl">1 % by weight. In certain embodiments as otherwise described herein, the ionic liquid is</p>

<p dir="rtl">10 In an amount in the range from 0.05 wt% to 10 wt%, e.g., 0.05 wt% to 8 wt%, or 0.05 wt% to 6 wt%, or 0.05 wt% to 4 wt%, or 0.05 wt% to</p>

<p dir="rtl">3 %by weight, or 0.05%by weight to 2%by weight, or 0.05%by weight to 1%by weight. In specimens</p>

Specifically as otherwise described herein, the catalyst composition comprises at least one ionic liquid in a total amount within the range of 0.1 wt% to 10 wt%, e.g., 0.1

<p dir="rtl">15 %by weight to 8%by weight, or 0.1%by weight to 6%by weight, or 0.1%by weight to 4%by weight, or 0.1%by weight to 3%by weight, or 0.1%by weight to 2%by weight, or 0.1%by weight to 1%by weight. In certain embodiments as otherwise described herein, the catalyst composition includes at least one ionic liquid in a total amount within the range of 0.2%by weight to 10%by weight, e.g., 0.2%by weight to 8%by weight, or 0.2%by weight to 6%by weight, or 0.2</p>

<p dir="rtl">20 %by weight to 4%by weight, or 0.2%by weight to 3%by weight, or 0.2%by weight to 2%by weight, or 0.2%by weight to 1%by weight. In certain embodiments as otherwise described herein, the catalyst composition includes at least one ionic liquid in a total amount within the range of 0.5%by weight to 10%by weight, e.g., 0.5%by weight to 8%by weight, or 0.5%by weight to 6%by weight, or 0.5%by weight to 4%by weight, or 0.5%by weight to 3%by weight, or 0.5%by weight</p>

<p dir="rtl">25 Up to 2% by weight.</p>

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A person of ordinary skill in the art will recognize that the term "ionic liquid" generally refers to a class of poorly coordinated salts having a relatively low melting point such as, for example, less than 100°C. In certain embodiments as otherwise described herein, the ionic liquid comprises a compound according to the formula:

[A]n+[Y]n- 5

where n is 1 or 2;

[n]Y- is selected from tetrafluoroborate BF4]-(tetrafluoroborate](hexafluorophosphate](PF6); dicyanoamide N(CN)2]-(dicyanamide](; halides I-, F-, Br-, Cl-); hexafluoroantimonate

<p dir="rtl">10 )-[SbF6](; nitrate]-(NO3); nitrite)-[NO2](; anionic metal complexes (e.g.,</p>

-2[AuCl4]-, [PdCl4]2-, [CuCl4](; acetate)-[CH3COO](; trifluoroacetate)-(F3CCOO]-([; hexafluoroarsenate]-(AsF6); sulfate

)-2[SO4](; hydrogen sulfate R′-SO4]-( hydrogen sulfate](; alkyl sulfate)-′[R -[SO4](; tosylate)-[C7H7SO3](; triflate)-[CF3SO3](; nonaflat)-[C4F9SO3](;

<p dir="rtl">15 Trifluoroethylene trifluorophosphate (3(PF3(C2F5)(; taricyanomethide)-[3(C(CN)(; taricyanoborate)-[4(B(CN)(; thiocyanate)-[SCN](; carbonate)-2[CO3](; carboxylate)-[R′-COO](; sulfonate)-[R′SO3](; dialkyl phosphate)-[″R′PO4R](; alkyl phosphonate)-[R′HPO3](; and bisulfonyl imide)-[R′-SO2)2N)]( )e.g., bis)trifluoromethylsulfonyl(imide)(; where 'R and R'</p>

<p dir="rtl">20 Each of them is individually an aliphatic or fatty cyclic alkyl with linear or branched C1–C12; an aryl with C5–C18; an alkyl with C1–C6 aryl substitution with C5–C18; or an aryl with C5–C18 alkyl substitution with C1–C6, the alkyl optionally substituted with one or more halogens;</p>

+[A] is chosen from the quaternary ammonium cations with the formula +[NR1R2R3R], the phosphonium cations with the formula

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+[PR1R2R3R], sulfonium cations with the formula +[SR1R2R], guanidinium cations with the formula:

،

Imidazolium cations with the formula:

<p dir="rtl">5 ،</p>

Wherein the imidazole is optionally substituted by one or more of the selected groups of alkyl with C1–C6; alkoxy with C1–C6; aminoalkyl with C1–C6; aryl with C5–C12; and alkyl with C1–C6 substituted by aryl with C5–C12; pyridinium cations having the formula:

10 ،

Wherein the pyridine is optionally substituted by one or more of the following groups: alkyl with C1–C6; alkoxy with C1–C6; aminoalkyl with C1–C6; aryl with C5–C12; and alkyl with C1–C6 substituted by aryl with C5–C12; the pyrazolium cations have the formula:

<img file="SA18210B1_D0001.tif" />

15 Wherein the p-arzole is optionally substituted with one or more of the following groups: alkyl with C1–C6; alkoxy with C1–C6; aminoalkyl with C1–C6; aryl with C5–C12; alkyl with C1–C6 substituted with C5–C12; and triazolium cations of the formula:

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<img file="SA18210B1_D0002.tif" />

Wherein the triazole is optionally substituted by one or more of the following groups: alkyl with C1–C6; alkoxy with C1–C6; aminoalkyl with C1–C6; aryl with C5–C12; and alkyl with C1–C6 substituted by aryl with C5–C12; wherein R1, R2, and R3 are each individually

<p dir="rtl">5 Hydrogen; alkyl having C1–C20; heteroaryl having C3–C8 optionally substituted with one or more alkyls having C1–C6 and a halogen; alkyl having C1–C6 substituted; heteroaryl having C3–C8, heteroaryl having one or more alkyls having C1–C6 optionally substituted with one or more alkyls having C1–C6 and a halogen; polyether having the formula CH2CH2O]nRa-] where n is in the range 1–50,000 and Ra is chosen from alkyl having C1–C20; aryl having C5–C12 optionally substituted</p>

<p dir="rtl">10 with one or more alkyls having C1–C6 and a halogen; and alkyls having C1–C6 with an aryl substitution having C5–C12, the aryl having one or more alkyls having C1–C6 and a halogen optionally substituted; wherein R is selected from alkyls having C1–C20; alkyls having C1–C6 with a heteroaryl substitution having C4–C8, the heteroaryl having one or more alkyls having C1–C6 and a halogen optionally substituted; and alkyls having C1–C6 with an aryl substitution having C4–C12, the aryl having</p>

<p dir="rtl">15 With one or more alkyl groups C1–C6 and a halogen.</p>

For example, in certain embodiments such as these, +A]n] is selected from 1-butyl-1-methylpyrrolidinium, 1-butyl-2,3-dimethylimidazolium, 1-butyl-3-methylimidazolium, 1-ethyl-3-methylimidazolium, 1-ethyl-3-methylpyridinium, 1-methyl-3-octylimidazolium, ethyldimethyl-)2-methoxyethyl(ammonium, taributylmethylammonium, taricyclohexyltatardecylphosphonium.

<p dir="rtl">20 In certain embodiments such as these, -Y]n] is selected from bis(t)trifluoromethylsulfonyl(imide), dicyanamide, ethyl sulfate, methyl phosphonate, methyl sulfate, octyl sulfate, tartracyanobate, tartracyanobate, tetrafluoroborate, tartracyanomethane, triflate, and tris(pentafluoroethyl)trifluorophosphate.</p>

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In certain embodiments as otherwise described herein, the at least one ionic liquid is selected from 1-butyl-3-methylimidazolium triflate, 1-ethyl-3-methylpyridinium ethyl sulfate, 1-butyl-1-methylpyrrolidinium triflate, 1-butyl-2,3-dimethylimidazolium triflate, 1-butyl-3-methylimidazolium tarecyanomethane, 1-butyl-3-methylimidazolium

<p dir="rtl">5 Methyl sulfate, 1-butyl-3-methylimidazolium octyl sulfate, 1-butyl-3-methylimidazolium tetrafluoroborate, 1-ethyl-3-methylimidazolium ethyl sulfate, 1-ethyl-3-methylimidazolium methylphosphonate, 1-ethyl-3-methylimidazolium triflate, 1-butyl-1-methylpyrrolidinium bis)t-trifluoromethylsulfonyl(imide), 1-butyl-1-methylpyrrolidinium tetrafluoroborate, 1-butyl-1-methylpyrrolidinium tris)pentafluoroethyl(t-trifluorophosphate, 1-butyl-3-methyl</p>

<p dir="rtl">10 Imidazolium bis(t)fluoromethylsulfonyl(imide), 1-butyl-3-methylimidazolium tricyanomethane, 1-ethyl-3-methylpyridinium bis(t)fluoromethylsulfonyl(imide), 1-ethyl-3-methylimidazolium tricyanoborate, 1-ethyl-3-methylimidazolium tris)pentafluoroethyl(t)fluorophosphate, 1-methyl-3-octylimidazolium triflate, ethyl dimethyl-)2-methoxyethyl(ammonium tris)pentafluoroethyl(t)fluorophosphate, tributylmethylammonium dicyanoamide, tricyclo</p>

<p dir="rtl">15 Hexyltetradecylphosphonium tris)pentafluoroethyl)trifluorophosphate, and 1-ethyl-3-methylimidazolium bis)trifluoromethylsulfonyl(imide).</p>

A person of ordinary skill in the art will recognize that other components may be present in the catalyst composition as otherwise described herein. However, in certain embodiments as otherwise described herein, the total amount of porous carrier material, palladium

<p dir="rtl">20 palladium, booster, ionic liquid at least 90 wt%, at least 92.5 wt%, at least 95 wt%, at least 97.5 wt%, at least 98 wt%, at least 99 wt%, at least 99.5 wt%, or at least 99.9 wt% of the catalyst composition.</p>

A person of ordinary skill in the art will recognize that the catalyst composition as otherwise described herein can be provided using conventional methods, for example, by one or more of the following:

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Impregnation steps comprising the impregnation (e.g., by pre-wetting or soaking in excess solution) of a porous carrier material with an impregnation solution comprising one or more ionic liquids or palladium and, optionally, a promoter (e.g., silver), each impregnation step being followed by a drying or calcination step.

In certain embodiments of the production of the catalyst composition described herein, the liquid is dissolved or suspended

<p dir="rtl">5 Ionic liquids or mixtures of several ionic liquids in a solution agent suitable for this purpose, such as for example water, alcohols, acetone etc., or in a solution agent mixture, and continuously applied to the already pre-formed catalyst inside the reaction chamber with the help of a nozzle. For this purpose the solution agent is continuously removed from the reaction chamber during the process. In order to achieve an even coating of the substrate, the substrate material is continuously fluidized by a process gas in a process known as fluidized bed coating. The</p>

<p dir="rtl">10 Other suitable painting processes are dip coating or spray application using a spray gun or spray drying gun.</p>

Apart from the application of ionic liquid by coating techniques, the same can be applied by impregnation with a solution or suspension. For this purpose, the ionic liquid or mixtures of several ionic liquids are dissolved or suspended in a suitable solution agent (mixture) and subsequently contacted with the pre-formed catalyst.

<p dir="rtl">15 Remove the solution agent under vacuum or at elevated temperature (or both), by keeping it in the air,</p>

Or by a gas stream. The amount of solution agent used can be equal to, smaller or larger than the pore size of the catalyst used.

The amount of ionic liquid used, in certain desired embodiments, is equal to or smaller than the pore size of the catalyst used. After application of the ionic liquid, one is left with an externally dry solid covered

<p dir="rtl">20 With the desired amount of ionic liquid. The pore size of the resulting catalyst composition is reduced by the volume of ionic liquid. For a total catalyst weight of 0.1–10 wt%, 0.2–6 wt% is preferable, and 0.3–4 wt% of ionic liquid is particularly preferable. The distribution of the ionic liquid on the substrate body in the form of a microscopic, granular or powder is freely adjusted by selecting the coating conditions. Depending on the selection of conditions, the formation of so-called eggshell, egg white, or</p>

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Egg, or uniform distribution of ionic liquid on the substrate. In addition, any concentration gradient of ionic liquid on the substrate can be created.

The ionic liquid is preferably applied to the substrate surface as a thin film. The thickness of the ionic liquid film on the substrate surface for the catalysts described herein is typically in the range of 10 to 2000 μm,

<p dir="rtl">5 Preferably within the range of 100 to 1000 micrometers, and particularly preferably within the range of 100 to</p>

800 Micrometer

The resulting catalyst can be used without restricting the target reaction. The removal of metal particles necessary to activate the catalyst can occur before or after ionic liquid coating.

The catalyst can for example be reduced, before or after the addition of the ionic liquid or a mixture of liquids.

<p dir="rtl">10 Ionic. The methods used for reduction are known to the expert and may include, for example, wet chemical methods with a reducing agent such as, for example, LiAlH4, NaBH4, hydrazine (hydrart), hypophosphate, formic acid, or their salts (formate). In addition, reduction may be induced in the gaseous phase using hydrogen (pure hydrogen or in a mixture containing hydrogen; preferably at a concentration of</p>

<p dir="rtl">15 Hydrogen greater than 1 mol % in N2 or other inert gases (within the temperature range of 20–200 °C, preferably at 50–150 °C).</p>

The reduced metal particles obtained in this way usually have a diameter within the range of 1 to 60 nm, preferably within the range of 1 to 30 nm, and particularly preferably within the range of 2 to 20 nm.

<p dir="rtl">20 Similarly, a hydrogenation catalyst may be desorbed after ionic liquid has been supplied to it, e.g., while in a bed in a reactor, by contact with a gas containing hydrogen as described above. For example, the ionic liquid may be impregnated on the catalyst in a catalyst synthesis process, the catalyst may then be shipped and stored at the process site, with desorbed catalyst bed in an acetylene desorbed reactor.</p>

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However, in other embodiments, the hydrogenation catalyst is not pre-extracted prior to contact with the process gas.

Prior to use, it may be useful to dry the catalyst to reduce the amount of any adsorbed water. Drying can be performed with a dry inert gas (e.g., nitrogen, hydrogen, residual methane, ethane) at a temperature (e.g., at least 50°C, e.g., in the range of

<p dir="rtl">5 100-50°C) for a period of time (e.g., five hours to two days) until the flowing current decreases.</p>

From the drying gas to below the desired dew point, e.g. below -60°C.

After any hydrogenation and drying steps, it is desirable to reduce the catalyst temperature to a temperature that is sufficient to start the reaction gas flow. The present inventors have determined that the catalysts described herein can be started, as a result of their high selectivity to acetylene (and hence the rate of

<p dir="rtl">10 The ethylene release is relatively low, at a relatively higher temperature. The catalyst starts to operate.</p>

Conventional catalysts (such as the catalyst C of the examples) typically operate at a lower temperature, 30°C or less. Significantly, the present inventors specify that the catalysts described herein may first be contacted with the process gas at higher temperatures, e.g., in the range of 31-50°C. In certain embodiments, the catalysts described herein may first be contacted with the process gas at a temperature in

<p dir="rtl">15 The range of 31-45°C, or 31-40°C. In such other embodiments, the catalyst described herein may be first contacted with the process gas at a temperature in the range of 35-50°C, e.g., 35-45°C, or 35-40°C. In such other embodiments, the catalyst described herein may be first contacted with the process gas at a temperature in the range of 40-50°C, e.g., 40-45°C, 31-40°C, or</p>

<p dir="rtl">20 Range from 35-40°C.</p>

Certain catalysts suitable for use in the methods described herein are described in U.S. Patent Application Publication No. 2013/0102819, which is incorporated herein by reference in its entirety.

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In various aspects and embodiments, the methods as otherwise described herein may be performed in a selective hydrogenation reactor having a catalyst bed or series of catalyst beds having a catalyst composition (e.g., a catalyst composition as otherwise described herein) capable of selectively hydrogenating acetylene.

.acetylene 5

In another aspect, the present inventors have specified that forward selective hydrogenation reactors can be started without many of the undesirable aspects of conventional methods (e.g., long time periods for sending the process gas to ignition, pre-charging the catalyst with carbon monoxide (CO), or adding CO to the process stream during start-up), even when the catalyst composition is “fresh” (e.g., newly synthesized or regenerated in the reactor, reduced or non-reduced, not exposed to

After gas treatment. As a person of ordinary skill in the art will realize, this startup process can desirable reduce material costs, reduce reactor downtime, and reduce reactor waste (i.e., the reactor output before the reactor is operating at full capacity).

Accordingly, another aspect of the disclosure is a method for starting a dehydrogenation reactor, reactor 15 having one or more catalyst beds each containing a catalyst suitable for the hydrogenation of acetylene.

Selectively in a process gas comprising at least 10 mole % of ethylene, at least 1 ppm of acetylene, at least 5 mole % of hydrogen (e.g., and at least 10 ppm of carbon monoxide (CO). The method includes providing each catalyst bed at not more than 20°C, the catalyst of the catalyst bed in contact with a first gas, the first gas being unreactive in the presence of the catalyst at the first temperature. In the presence of the first gas, each catalyst layer is heated to at least a second temperature, the second temperature being at least 10 degrees higher (e.g., at least 20 degrees higher, at least 30 degrees higher, at least 40 degrees higher, at least 50 degrees higher, or even at least 60 degrees higher) than the first temperature, the first gas being unreactive in the presence of the catalyst at the second temperature. The composition of the gas is changed in contact with the catalyst in each layer.

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From the first gas to the process gas stream while the catalyst bed is at least the second temperature. The process gas is allowed to flow through each catalyst bed until the acetylene concentration at the reactor outlet (i.e., serving as the outlet for the reacting process gas) is less than 1 ppm (e.g., less than 0.5 ppm). Thus, the temperature of the catalyst bed can be increased when it is in contact with

<p dir="rtl">5 With the first gas,</p>

such that the process gas does not need to be converted for ignition while the catalyst beds reach temperature. In certain embodiments, the acetylene concentration at the reactor outlet does not exceed 1 ppm within 6 hours, e.g., within 5 hours, within 4 hours, within 3 hours or even within 2 hours of the process gas being introduced into one or more of the catalyst beds.

<p dir="rtl">10 Catalyst. The catalyst materials described herein may allow the introduction of process gas while</p>

The catalyst bed(s) are at an elevated temperature, which reduces the amount of process gas flowing through the catalyst bed(s) during start-up.

In another aspect (in combination with the aspect described above or separately), the disclosure provides a method for starting a selective hydrogenation reactor without pretreatment.

<p dir="rtl">15 For the catalyst with CO and without adding CO to the process gas. For example, in one embodiment,</p>

A method for starting a selective hydrogenation reactor as described above provides the reactor with each catalyst bed having a catalyst in contact with a first gas, the first gas being unreactive in the presence of the catalyst at the initial temperature, where the catalyst in the reactor is not in contact with a gas containing carbon monoxide which increases the concentration of carbon monoxide

<p dir="rtl">20 monoxide of about 100 ppm. The process gas stream is then introduced into the one or more catalyst beds. Crucially, the method includes refraining from adding carbon monoxide to the process gas. Accordingly, the method is carried out without adding significant amounts of carbon monoxide (CO) to the process (i.e., by pretreatment or by adding a process gas). The present inventors have specified that the use of catalysts</p>

<p dir="rtl">25 The described in this application can allow operation without carbon monoxide,</p>

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Which can represent significant improvements in safety, process complexity and process costs. In certain embodiments, these processes also include raising the catalyst bed temperature of each catalyst bed from no more than a first temperature to at least a second temperature. The catalyst bed temperature(s) may be raised before or after the introduction of the process gas. In other embodiments, the process gas is introduced while the catalyst bed is being raised.

<p dir="rtl">5 Catalyst bed temperature(s). After the temperature is raised, the process gas may be flowed through one or more catalyst beds until the reactor effluent has less than 1 ppm acetylene (e.g., less than 0.5 ppm acetylene).</p>

The first temperature may represent, for example, the operating temperature of the reactor, for example, the temperature of the reactor system when it is not connected. In certain embodiments, the temperature does not increase

<p dir="rtl">10 The first temperature is above 50°C, for example, in the range of 31-50°C, 35-50°C, 40-50°C, or 45-50°C. In certain embodiments, the first temperature is not higher than 45°C, for example, in the range of 31-45°C, 35-45°C, or 45-40°C. In certain embodiments, the first temperature is not higher than 40°C, for example, in the range of 31-40°C, or 35-40°C. But in other embodiments,</p>

<p dir="rtl">15 The initial temperature is cooler, for example, no more than 30°C or even, in some models, no more than 25°C.</p>

The second temperature may, for example, represent the operating temperature of the reactor, i.e., the temperature at which the reactor effluent (for the specific process gas and other conditions being used) has an acetylene concentration of not more than 1 ppm (e.g., not more than 0.5 ppm).

<p dir="rtl">20 Thus, the second temperature may be the temperature of the hydrogenation reaction as described above. In certain embodiments, the second temperature is within the range of 40°C to 140°C. In certain desirable embodiments, the second temperature is within the range of 40°C to 100°C, e.g., 40°C to 90°C, or 50°C to 90°C. However, other second temperatures are possible. In some embodiments, the temperature is</p>

<p dir="rtl">25 The second is within the range of 20°C to 130°C, for example, in the range of 20°C</p>

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120°C to 120°C, 20°C to 110°C, 20°C to 100°C, or 20°C to 90°C.

In some embodiments, the second temperature is within the range of 40°C to 140°C, e.g., 40°C to 130°C, or 40°C to 120°C, or

<p dir="rtl">5 40°C to 110°C. In some models, the second temperature is within</p>

The range is from 50°C to 140°C, e.g., 50°C to 130°C, or 50°C to 120°C, or 50°C to 110°C. In some embodiments, the second temperature is within the range from 60°C to 140°C, e.g., 60°C to 130°C, or 60°C to 120°C, or 60°C to

<p dir="rtl">10 110°C to 100°C, 60°C to 100°C, or 60°C to 90°C. The methods described herein can also be used with large differences between the first and second temperatures, e.g., at least 30°C, at least 40°C, at least 50°C or even at least 60°C.</p>

A temperature rise from no more than the first temperature to at least the second temperature can be carried out relatively quickly. For example, in certain embodiments as described

Otherwise in this application, the temperature of each catalyst layer is raised from no higher than the first temperature to at least the second temperature over a period of time not exceeding 10 hours, e.g., not exceeding six hours, e.g., in the range of 2-10 hours, 4-10 hours, or 3-6 hours. The temperature rate change can be, for example, in the range of 3-15 degrees

<p dir="rtl">20 Celsius/hour, for example, in the range of 3-12°C/hour, or 6-15°C/hour, or 6-12°C/hour.</p>

As described above, the process gas includes ethylene, acetylene, and hydrogen. The process gas may contain amounts of these materials and any other components as otherwise described in any embodiment herein. In certain embodiments, the process gas includes

<p dir="rtl">25 Treatment of at least 10 parts per million of carbon monoxide (CO).</p>

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The first gas is non-reactive, as described above. In certain embodiments, the first gas includes no more than 1 ppm of acetylene (e.g., more than 0.5 ppm). A variety of materials may be used as the first gas, individually or in a mixture. The first gas is non-reactive on the catalyst bed at the first temperature and the second temperature. Accordingly, the first gas in certain embodiments may include low amounts of (or no) hydrogen.

and/or low amounts (or no) of releasable hydrocarbon. In certain embodiments, the first gas comprises less than 2% hydrogen, e.g., less than 1% hydrogen. Gases such as nitrogen and fuel gas may be used.

In the various methods described above, each catalyst bed is changed from contact with the first gas to contact with the 10 process gas. The first gas can exist in the reactor at a pressure relatively lower than the process gas source, so that when the process gas is introduced into the reactor without opening the reactor outlet, it can mix with the first gas to provide a total reaction pressure. Desirably, the difference in pressure values ​​is small enough that the process gas is significantly diluted when it is first introduced into the reactor. For example, in one example of an embodiment, the first gas pressure in the reactor could be 1.3815-2.07 MPa, while the process gas pressure could be 2.76-3.45 MPa. Once

Mixing the primary gas and process gas in the reactor, the flow can be created by allowing the gas to leak out of the reactor. Of course, a person with ordinary skill in the art will realize that the specific method of introducing the process gas into the reactor will depend on the reactor design and process.

In certain desired embodiments as otherwise described herein, the process gas 20 itself may be used to pressurize the reactor to the reactor pressure at which the selective hydrogenation is to be operated. That is, in certain embodiments, no pre-pressure with an inert gas to the process pressure is required. Instead, the process gas may be used to bring the reactor up to the process pressure. Advantageously, the high selectivity of the catalysts described herein allows the process gas to provide the reactor pressure with much lower risk of thermal runaway.

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The present inventors have determined that the catalysts described herein can process the temperature more quickly than previous catalysts due to the high selectivity for the hydrogenation of acetylene. Accordingly, another aspect of the disclosure is a method for starting a selective hydrogenation reactor, the reactor having one or more catalyst beds each containing a suitable catalyst

<p dir="rtl">5 For selectively hydrogenating acetylene in a process gas comprising at least 10 mole % of ethylene, at least 1 ppm of acetylene, and at least 5 mole % of hydrogen, the method comprising providing each catalyst bed at not more than a first temperature, the catalyst of the catalyst bed being in contact with the gas; in the presence of the process gas, heating each catalyst bed to at least a second temperature, the second temperature being at least 20°C higher</p>

<p dir="rtl">10 From the first temperature, each catalyst bed is heated at a rate in the range of at least 3°C/h; and the process gas is allowed to flow through the catalyst bed until the acetylene concentration at the reactor outlet is less than 1 ppm. In certain embodiments, the rate is in the range of 3-20°C/h, e.g., 3-15°C/h or 3-12°C/h. In certain embodiments, the rate is in the range of 6-20°C/h, e.g.,</p>

<p dir="rtl">15 15-6°C/h or 6-12°C/h. In certain models, the rate is</p>

The range is 9-20°C/h, eg 9-15°C/h.

The catalysts described above in connection with the hydrogenation methods may be suitable for use in the start-up methods described in this application.

Conventionally, the methods described herein may further include, prior to introducing the treatment gas 20 into the bed or contacting the catalyst composition with the treatment gas, reducing the catalyst (e.g., with a flow of

A gas containing hydrogen.

Another aspect of the disclosure is a hydrogenation catalyst composition including a porous carrier, present in the composition in an amount within the range of 90 wt% to 99.9 wt%; palladium, present in the composition in an amount within the range of 0.02 wt% to 0.5 wt% (e.g., 0.04 wt% to 0.15 wt%),

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calculated on an elemental mass basis; and one or more ionic liquids, present in the composition in a combined amount of up to 10 wt%. In certain embodiments, the catalyst composition further includes at least one promoter (e.g., silver), present in the composition in an amount within the range of 0.05 wt% to 0.25 wt%, e.g., 0.08 wt% to 0.25 wt%, or 0.1 wt% to 0.25 wt%, calculated on an elemental mass basis.

The amount of palladium in the catalyst composition may, for example, be within the range of 0.05 wt% to 0.2 wt%, 0.05 wt% to 0.15 wt%, 0.07 wt% to 0.2 wt%, 0.07 wt% to 0.15 wt%, 0.08 wt% to 0.2 wt%, 0.08 wt% to 0.15 wt%, 0.1 wt% to 0.2 wt%, 0.1 wt% to 0.2 wt%, 0.1 wt% to 0.15 wt%, 0.1 wt% to 0.10 wt%, 0.11 wt% to 0.2 wt%, or 0.11 wt% to 0.15 wt%.

% by weight. The present inventors have determined that a catalyst containing relatively large amounts of palladium can advantageously provide high conversion and high selectivity without runaway.

Another aspect of the disclosure is a hydrogenation catalyst composition including a porous carrier, present in the composition in an amount within the range of 90 wt% to 99.9 wt%; palladium, present in composition 15 in an amount of at least 0.02 wt% (e.g., 0.04 wt% to 0.15 wt%), calculated

On an elemental mass basis; and one or more ionic liquids, present in the composition in a combined amount of up to 10 wt%. In certain embodiments, the catalyst composition further includes at least one promoter (e.g., silver), present in the composition in an amount within the range of 0.05 wt% to 0.25 wt%, e.g., 0.08 wt% to 0.25 wt%, or 0.1 wt% to 0.25 wt%, calculated on a 20 elemental mass basis. In this aspect, the carrier has a BET surface area of ​​not more than 10

m2/g, and a pore volume of at least 0.1 mL/g. The BET surface area and pore volume of the carrier material may otherwise be as described above.

Another aspect of the disclosure is a hydrogenation catalyst composition including: a porous carrier, present in the composition in an amount within the range of 90 wt% to 99.9 wt%; palladium, present in composition 25 in an amount within the range of at least 0.02 wt%, calculated on an elemental mass basis; and one

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or more ionic liquids, present in the composition in a combined amount of up to 10 wt%, wherein the hydrogenation catalyst has a BET surface area of ​​not more than 10 m2/g and a pore volume of at least 0.05 mL/g. The present inventors have determined that impregnation with a relatively small ionic liquid can provide a large volume of residual pores in the catalyst, i.e., the pores accessible by the 5 mercury porosity gauge are not completely filled.

In certain embodiments such as these, the hydrogenation catalyst composition comprises palladium in an amount of 0.03

% by weight at least, or 0.04 % by weight at least, or 0.05 % by weight at least, or 0.06

% by weight at least, or 0.07 % by weight at least, or 0.08 % by weight at least, or 0.09

% by weight at least, or 0.1 % by weight at least, or 0.11 % by weight at least, or 0.12

<p dir="rtl">10 % by weight at least, or 0.13 % by weight at least, or 0.14 % by weight at least, or 0.15</p>

% by weight at least. In certain such embodiments, the hydrogenation catalyst composition comprises palladium in an amount of not more than 0.5 wt % (e.g., more than 0.4 wt %, not more than 0.3 wt %, or not more than 0.2 wt %). For example, various embodiments comprise palladium in an amount within the range of 0.02 wt % to 0.5 wt %, 0.02 wt % to 0.45 wt %, 15 or 0.03 wt % to 0.4 wt %, 0.03 wt % to 0.35 wt %, 0.04 wt % to 0.3 wt %, or 0.04 wt % to 0.25 wt %.

These hydrogenation catalysts may advantageously include a booster as otherwise described herein.

In certain desirable embodiments, such hydrogenation catalysts have a 20 BET surface area in the range of 2 m2/g to 10 m2/g, e.g.,

Within the range of 2 m2/g to 9 m2/g, or 2 m2/g to 8 m2/g, or 2 m2/g to 7 m2/g, or 2 m2/g to 6 m2/g, or 2 m2/g to 5 m2/g, or 3 m2/g to 10 m2/g, or 4 m2/g to 10 m2/g, or 5 m2/g to 10 m2/g, or 6 m2/g to 10 m2/g, or 2

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m2/g to 6 m2/g, or 3 m2/g to 7 m2/g, or 4 m2/g to 8 m2/g, or 5 m2/g to 9 m2/g.

In certain desirable embodiments, such hydrogenation catalysts have a pore size in the range of 0.05 mL/g to 1.0 mL/g, e.g., 0.05 mL/g to 0.4 mL/g.

<p dir="rtl">5 liter/g. In certain embodiments such as these, the hydrogenation catalyst has a pore size in the range of 0.10 ml/g to 1.0 ml/g, e.g., 0.10 ml/g to 0.80 ml/g, or 0.10 to 0.60 ml/g, or 0.10 to 0.40 ml/g, or 0.10 to 0.30 ml/g, or in the range of 0.20 ml/g to 1.0 ml/g, e.g., 0.20 ml/g to 0.80 ml/g, or 0.20 to 0.60 ml/g, or 0.20 to 0.40 ml/g, or 0.20 to 0.35 ml</p>

<p dir="rtl">10 litre/g, or in the range from 0.40 ml/g to 1.0 ml/g, e.g., 0.40 ml/g to 0.80 ml/g, or 0.40 to 0.60 ml/g.</p>

Desirably, the catalyst according to the disclosure includes an ionic liquid in an amount that does not completely fill the pore volume of the carrier. For example, in certain embodiments as otherwise described herein, the difference between the pore volume of the carrier and the pore volume of the catalyst (i.e., including palladium

<p dir="rtl">15 palladium, i.e., the ionic liquid and the booster) in the range of 10-90% of the pore volume of the carrier. In certain such embodiments, the difference is in the range of 20-90% of the pore volume of the carrier, e.g., 30-90% or 40-90%. In certain such embodiments, the difference is in the range of 10-80% of the pore volume of the carrier, e.g., 20-80%, 30-80%, or 40-80%. In certain such embodiments, the difference is in the range of 10-70% of the pore volume of the carrier, e.g., 20</p>

<p dir="rtl">20 70%, 30-70%, or 40-70%. In certain models like this, the difference is in the range of 10-</p>

60% of the pore volume of the carrier material, e.g., 20-60%, 30-60%, or 40-60%.

The catalysts according to the disclosure may include a variety of amounts of ionic liquid. For example, in certain embodiments as otherwise described herein, the ionic liquid is present in an amount in the range of 0.1 wt% to 10 wt%, e.g., 0.1 wt% to 8 wt%, or 0.1

<p dir="rtl">25 %by weight to 6%by weight, or 0.1%by weight to 4%by weight, or 0.1%by weight to 3%by weight,</p>

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Or 0.1% by weight to 2% by weight, or 0.1% by weight to 1% by weight, for example, 0.2% by weight to 3% by weight, or 0.5-4% by weight.

Catalysts according to these aspects of the disclosure may be otherwise as described above in relation to catalysts useful in the methods of the disclosure. Furthermore, catalysts according to this 5 aspect of the disclosure may be used in any methods as otherwise described herein.

The processes and materials described herein can be particularly useful in front-end applications. However, a person of ordinary skill in the art will recognize that they can be useful in a variety of other applications, particularly those where the risk of escape (e.g., due to high hydrogen concentrations) is a problem.

<p dir="rtl">10 Examples</p>

The following examples are illustrative of specific forms of the scavenger hunt, and their various uses. They are provided for illustrative purposes only, and should not be considered to be limiting to the scavenger hunt.

Example 1. Preparation of selective hydrogenation catalyst

A porous alpha-alumina carrier (4-mm discs) having a BET surface area of ​​5 ± 2 15 m2/g was impregnated with aqueous solutions of silver salt and palladium salt and calcined at at least 260 °C in air for 2 h. The silver content of the silver salt aqueous solution and the palladium content of the palladium salt solution were adjusted to make the final calcined impregnated carrier contain 0.050 ± 0.005 wt% palladium and 0.070 ± 0.005 wt% silver. Palladium was placed within the outer 500 μm of a 20 m porous carrier. The pore volume of the metal-saturated carrier was 0.26 mL/g.

The calcined saturated carrier was also impregnated with an aqueous solution of about 0.5 wt% of ionic liquid (IL) on the dry saturated carrier. The remaining material was dried at 150 °C for 2 h to provide catalyst A1. The catalyst had a pore volume of 0.23 mL/g.

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Catalyst A2 was prepared in a manner similar to that of catalyst A1. A comparable catalyst was also provided.

C, does not contain IL and has a much lower Pd load than catalysts A1 and A2.

Table 1. Catalyst composition

<tr><td><p dir="rtl">IL (% by weight)</p></td><td><p dir="rtl">Ag (% by weight)</p></td><td><p dir="rtl">Pd (% by weight)</p></td><td><p dir="rtl">number</p></td></tr><tr><td><p>0.5</p></td><td><p>0.07</p></td><td><p>0.05</p></td><td><p>A1</p></td></tr><tr><td><p>0.5</p></td><td><p>0.11</p></td><td><p>0.08</p></td><td><p>A2</p></td></tr><tr><td><p>0.0</p></td><td><p>0.05</p></td><td><p>0.02</p></td><td><p>C</p></td></tr>

Example 2. Selective hydrogenation

<p dir="rtl">5 The catalysts prepared according to Example 1 were placed in a 15 ml catalyst bed in a reactor tube. The catalyst was evaporated in a hydrogen flow with a vacuum gas rate of &lt;500 h-1 at 94 °C for 1 h before the feed gas mixture was introduced into the reactor. A gas mixture containing 200 ppm of carbon monoxide (CO), 19 MONOXIDE (0.35 mol% of H2), and 30 mol% of C2H2 was passed through the reactor.</p>

<p dir="rtl">10 45, (C2H4)ETHYLENE% in moles of CH4 and nitrogen in equilibrium above the catalyst bed at a speed of</p>

Gas Hourly Space Velocity (GHSV) was 7,000 h-1, with a total pressure of 3.45 MPa. The catalyst bed was heated using a water bath, at intervals of 2–5 °C, starting at 40 °C. The concentration of acetylene and ethane at the reactor outlet was monitored, and is shown in Fig. 1.

<p dir="rtl">15 As shown in Figure 1, the temperature at which the acetylene concentration at the reactor outlet drops to 25 ppm (i.e., the activity index; T1) is similar for catalysts A1 and C, but the operating window of catalyst A1 (i.e., the difference between the escape temperature, T2 (the temperature at which the ethane concentration at the reactor outlet reaches 2 mol%)) and T1 is much larger than that of catalyst C—71 °C versus 21 °C, respectively.</p>

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Example 3. Carbon Monoxide (CO) Swing Test

The catalysts prepared according to Example 1 were placed in a 15 ml catalyst bed in a reactor tube. The catalyst was evaporated in a hydrogen flow with a gas vacuum rate of &lt;500 h-1 at 94 °C for 1 h before the feed gas mixture was introduced into the reactor.

<p dir="rtl">5 A gas mixture containing 200 ppm of carbon monoxide (CO), 0.5 mole % of monoxide, 19 mole % of C2H2, 26 mole % of H2, 40 mole % of ethylene (C2H4), and equilibrium nitrogen is placed over the catalyst bed at a gas hourly space velocity (GHSV) of 7,000 h-1. The catalyst bed is heated to a temperature sufficient to provide an acetylene concentration of 20–30 ppm.</p>

<p dir="rtl">10 In million at the reactor outlet. The ethylene selectivity of the process was continuously monitored at the reactor outlet and is shown in Figure 2.</p>

At 25 and 45 h on stream, the CO (carbon monoxide) concentration of the gas mixture was briefly reduced to 60 ppm, without reducing the reactor bed temperature. At 285 h on stream, the CO (carbon monoxide) concentration was increased

<p dir="rtl">15 MONOXIDE of the gas mixture was increased to 340 ppm, and the reactor bed temperature was adjusted to provide 95% acetylene conversion. The carbon monoxide (CO) concentration was subsequently reduced to 60 ppm, and then increased to 200 ppm. At 308 h on stream, the cycle was repeated at 285 h on stream. The results, shown in Fig. 2, show that the ethylene selectivity of catalyst A1 was restored after variations in CO concentration.</p>

<p dir="rtl">20 The selectivity of catalyst A1 (CO) is much better than that of catalyst C. Moreover, the results show that the selectivity of catalyst A1 remains higher than that of catalyst C at both high and low concentrations of carbon monoxide (CO).</p>

Example 4. Selective hydrogenation

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The catalysts prepared according to Example 1 were placed in a 15 ml catalyst bed in a reactor tube. The catalyst was evaporated in a hydrogen flow with a gas velocity of &lt;500 h-1 at 94 °C for 1 h before the feed gas mixture was introduced into the reactor. A gas mixture containing 350 ppm of carbon monoxide (CO) was placed

<p dir="rtl">5 17, MONOXIDE 0.69% mole of H2, 47% mole of C2H2, ethylene 0.5% mole of C2H2</p>

<p dir="rtl">11 ,(C2H4)ETHYLENE 4 mole %, CH4 4 mole %propylene, 0.098 ppm propadiene, 0.13 ppm methyl acetylene, and 130 ppm 1,3-butadiene were deposited over the catalyst bed at a gas hourly space velocity (GHSV) of either 4,500 h-1 or 13,000 h-1, with a total pressure of 3.45 MPa. The catalyst bed was heated using a water bath, at intervals ranging from 5 °C. The acetylene conversion and ethylene selectivity were continuously monitored at the reactor outlet and are shown in Figure 3. Remarkably, the concomitant increase in temperature required to maintain the desired acetylene conversion at 13,000 h-1 gas velocity in</p>

<p dir="rtl">15 The GAS HOURLY SPACE VELOCITY (GHSV) relative to 4,500 h-1 is 10–12 °C for catalyst C, but only 8–10 °C for catalyst A1. Furthermore, at 13,000 h-1, the ethylene selectivity of catalyst A1 remained above 95% when acetylene conversion was as high as 95%, and the ethylene selectivity of catalyst A1 remained above 50% when acetylene conversion was maintained above 99%.</p>

<p dir="rtl">20 Example 5. Selective hydrogenation</p>

The catalysts prepared according to Example 1 were placed in a 15 ml catalyst bed in a reactor tube. The catalyst was evaporated in a hydrogen flow with a gas vacuum rate of &lt;500 h-1 at 94 °C for 1 h before the feed gas mixture was introduced into the reactor. While the gas mixture containing 200 ppm of carbon monoxide (CO) was placed

<p dir="rtl">25 19, MONOXIDE 0.35% mole of H2, 30% mole of C2H2, ethylene 30% mole of C2H2</p>

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<p dir="rtl">45 ,(C2H4)ETHYLENE mole % of CH4 and equilibrium nitrogen over the catalyst bed at a gas hourly space velocity (GHSV) of either 7,000 h-1 or 28,000 h-1, with a total pressure of 3.45 MPa. The catalyst bed was heated using a water bath, at intervals of 2–5 °C, starting at 40 °C. The acetylene conversion and ethylene selectivity were continuously monitored at the reactor outlet, and are shown in Fig. 4. Remarkably, the ethylene selectivity of catalyst A2 at 28,000 h-1 was similar to that of catalyst C only at 7,000 h-1, i.e., the process capacity was about 4 marts higher than that of catalyst A2.</p>

Example 6. Starting the reactor without pre-treatment of carbon monoxide (CO)

MONOXIDE 10

Commercial forward selective hydrogenation plants typically require pretreatment of the catalyst bed with carbon monoxide (CO) at startup to prevent the reactor temperature from running out when the process gas is first introduced into the reactor due to the non-selective hydrogenation of ethylene to ethane.

<p dir="rtl">15 A series of operating tests were conducted in a laboratory-scale test unit using the A1 catalyst without CO pretreatment and compared to the base case with CO pretreatment gas to the catalyst. The tests were conducted at gas hourly space velocity (GHSV) values ​​of 7000 h-1.</p>

The comparative start-up process in the laboratory scale test involved H2 removal at 94°C 20 for 1 h followed by purging with a pre-treatment of carbon monoxide (CO).

MONOXIDE Before all feed gases were introduced into the stream. In this comparative test, 1% CO in CH4 gas was used to purge the system for 20 min at 30 °C and to pressurize the reactor to 3.5 MPa, after which the feed gas containing 0.02% CO (CO), 3500 ppm H2, 20% CARBON MONOXIDE (CO), and 27% C2H2 was introduced.

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Ethylene (C2H4) was in the stream at 3.5 MPa. The water bath temperature was kept at 30 °C, while the top and bottom temperatures of the catalyst bed were monitored during the test. The data are shown in Figure 5. The first temperature point was when the pressure rise started with CH4/CO only.

<p dir="rtl">5 The pressure rise with CH4/CO took about 1-2 min. Initially, there was a brief heat loss of 2-3 °C for ~5 min. Feed gas introduction at 30 °C and 3.5 MPa did not cause significant heat loss. A sample of the reactor outlet gas was analyzed at 15 min after the catalyst bed temperature had stabilized. The outlet ethane concentration was constant at 120 ppm, which was from the stream</p>

<p dir="rtl">10 Input feed.</p>

The test run was then repeated in substantially the same manner, but replacing the CH4/CO pretreatment with N2 pretreatment, followed by introduction of feed gas at atmospheric pressure and reactor pressure with feed gas at a flow rate of 7000 GHSV (gas hourly).

<p dir="rtl">15 SPACE VELOCITY. The water bath temperature was kept at 30°C, and the peak and base temperatures were monitored during the test. It took about ~10 minutes to reach a target pressure of 3.5 MPa. The data are shown in Figure 6.</p>

During the 10 min compression period, a heat dissipation of 2 to 3 °C was observed, and both the top and bottom temperatures returned to below 30 °C after the gas flow stabilized at 3.5

<p dir="rtl">20 MPa, when the reactor outlet gas sample was analyzed it showed more than 2% ethane. The initial ethane formation was due to the fact that there was no flow from the reactor during the pressure rise before the reactor reached 3.5 MPa. Continued analysis of the outlet sample after the inlet and outlet flows stabilized at 3.5 MPa showed that the ethane content at the reactor outlet decreased to about 120 ppm, indicating no sustained ethane formation in the reactor.</p>

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Another test run was performed, this time with the N2 purge omitted between the hydrogen reduction and the feed gas introduction. Instead, the catalyst was purged with a feed gas containing 0.02% carbon monoxide (CO), 3500 ppm C2H2, 20% ethylene (C2H4), for 20 min before being compressed to 3.5 MPa5 with the feed gas. This was done to simulate the recirculation of gases prior to operation at plant conditions. Temperature measurements began at the onset of pressure rise; the data are shown in Fig. 7. No change in temperature was observed during the 20 min purge of the feed stream. Both the peak and base temperatures began to increase during the pressure rise and the peak temperature slightly exceeded the base temperature. The ethane formation during the temperature rise was about 10%. The 10 temperatures eventually returned to normal after 10 min. The ethane formation continued to decrease throughout the test until it stabilized at 120 ppm.

Finally, the operation procedure with the feed gas for purge as described above was applied to catalyst C. Figure 8 shows the changes of the catalyst bed temperature and ethane composition during the operation test. The temperature measurements started immediately after the feed was introduced. The peak temperature started to increase 15 °C before the pressure rise, and exceeded the base temperature at the beginning of the pressure rise. The peak temperature decreased slightly after the pressure rise and a continuous gas flow was established, but then continued to increase until it stabilized at 36 °C. The peak temperature never returned to below 30°. The ethane composition during this time was stable at ~16%, indicating continued runaway thermal activity.

.thermal runaway

<p dir="rtl">20 Thus, the operating experiments described above demonstrate that catalysts including ionic liquids can provide low thermal runaway risks, even in the absence of CO pretreatment.</p>

.CARBON MONOXIDE

Example 7. Insensitivity to carbon monoxide concentration

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A study was conducted on the sensitivity to carbon monoxide concentration under isothermal conditions. Remarkably, the selectivity of catalyst A1 was relatively sensitive to carbon monoxide concentration, while that of catalyst C was much more sensitive to carbon monoxide concentrations. In isothermal systems, the exothermic removal of excess heat from ethylene hydrogenation

<p dir="rtl">5 Ethylene with lower CO concentrations leads to reduced selectivity, resulting in exothermic runaway. Significantly, these data demonstrate that the catalysts described herein can be used under a wide variety of conditions even at low CO concentrations.</p>

The details given in this application are for example and for the purposes of illustrative discussion of the models.

<p dir="rtl">10 The present invention is preferred only and is presented when what is believed to be the most useful and easily understood description of the principles and conceptual aspects of the various embodiments of the invention is given. In this respect, no attempt has been made to show the structural details of the invention in more detail than is necessary for a basic understanding of the invention, and the description taken with drawings and/or examples shows those skilled in the art how the many forms of the invention can be incorporated into practice. Accordingly, before describing the processes and apparatus disclosed,</p>

<p dir="rtl">15 It should be understood that the aspects described in this application are not limited to specific models, devices, or bodies, and as such may of course vary. It is also understood that the terms used in this application are for the purpose of describing certain aspects only, and unless specifically defined in this application, are not intended to be limiting.</p>

The terms "a", "an", "the" and similar devices used in the context of describing the invention should be interpreted.

<p dir="rtl">20 (particularly in the context of the following claims) as including both the singular and the plural, unless otherwise indicated in this application or clearly conflicting with the context. The listing of value ranges in this application is intended only as a shorthand way of individually indicating each separate value within the range. Unless otherwise indicated in this application, each individual value is combined in the specification as if it were listed individually in this application. Ranges in this application may be expressed from “about” a value</p>

<p dir="rtl">25 one particular value, and/or "about" another particular value. When such a range is expressed, the side includes</p>

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Another from a given value and/or to another given value. Likewise, when values ​​are expressed approximately, using the preceding word "about", it will be understood that the given value constitutes another aspect. It will also be understood that the endpoints of each range are significant both in relation to the other endpoint and independently of the other endpoint.

<p dir="rtl">5 All methods described in this application may be performed in any appropriate order of steps unless otherwise stated in this application or clearly conflicts with the context. The use of any and all examples or illustrative language (e.g., “such as”) contained in this application is intended only to better illustrate the invention and does not impose a limitation on the scope of the otherwise claimed invention.</p>

No language in the specification should be construed as referring to any element not claimed for protection. Essential 10 for the practice of the invention.

Unless the context clearly requires otherwise, throughout the description and claims, the words “includes,” “includes,” and the like shall be construed in a comprehensive rather than exclusive or encompassing sense; that is, in the light of “including, but not limited to,” words that use a singular or plural number shall also include a plural and singular number, respectively. In addition, the words “in this application” shall indicate

<p dir="rtl">15 “Above,” “below” and words of similar significance, when used in this application, refer to this application as a whole and not to any particular parts of the application.</p>

As would be understood by a person of ordinary skill in the art, each embodiment disclosed herein may include, or essentially consist of, or consist of a specific element, step, basic element or component thereof. As used herein, the term transition

<p dir="rtl">20 "Comprises" or "includes" means includes, but is not limited to, and allows for the inclusion of unspecified elements, steps, essential elements or components, even in significant quantities. The transitional phrase "consists of" excludes any unspecified element, step, essential element or component. The transitional phrase "consists primarily of" also limits the scope of the Model to those elements, steps, essential elements or components that are specified and do not materially affect the Model.</p>

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Unless otherwise indicated, all figures expressing quantities of components and properties such as molecular weight, reaction conditions, etc. used in the specification and claims are to be understood as modified in all cases by the term "about". Accordingly, unless otherwise indicated, the numerical parameters given in the specification and claims are approximate estimates that may vary depending on the 5 desired properties sought to be obtained by the present invention. At the very least, and not as an attempt to limit the application of the principle of equivalents within the scope of the claims, each numerical parameter should at least be interpreted in the light of the number of significant figures contained and by applying normal rounding techniques. Where further clarification is required, the term "about" has the meaning reasonably attributed to it by a person skilled in the art when used in conjunction with a numerical value or a specified range, i.e., indicating somewhat more or 10 somewhat less than the stated value or a range within the normal ranges of uncertainty and imprecision in the art.

Although the numerical ranges and parameters that define the wide range of the invention are approximations, the numerical values ​​shown in the specific examples are given as accurately as possible. However, any numerical value inherently contains certain errors that necessarily result from the standard deviation 15 present in the respective test measurements.

The combinations of elements or alternative embodiments of the invention disclosed herein shall not be construed as limitations. Each member of the combination may be referred to and claimed individually or in any combination with other members of the combination or other elements contained herein. It is anticipated that one or more members of the combination may be included or omitted from the combination for reasons of convenience and/or patentability. When such inclusion or omission occurs, the specification shall be deemed to contain

The set as modified thus meets the written description of all Markush sets used in the enclosed protective elements.

Certain embodiments of this invention are described in this application, including the best method known to the inventors for carrying out the invention. Of course, the differences in these described embodiments will become apparent to those of ordinary skill in the art when reading the foregoing description. The inventor expects that skilled craftsmen will use such

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These variations are as needed, and the inventors intend to practice the invention other than as specifically described in this application. Accordingly, this invention includes all modifications and equivalents of the subject matter described in the claims attached hereto as permitted by applicable law. Furthermore, any combination of the above described elements is included in all variations

<p dir="rtl">5 Potentially by selection unless otherwise stated in this application or clearly conflicts with the context.</p>

Furthermore, references to patents and printed publications are made throughout this specification. Both references and printed publications are incorporated herein by reference in full.

In conclusion, it is understood that the models of the innovation disclosed in this application illustrate the principles of innovation.

<p dir="rtl">10 The present. Other modifications that may be used are within the scope of the invention. Thus, by way of example, but not limited to, alternative bodies to the present invention may be used in accordance with the instructions contained herein. Accordingly, the present invention is not limited to that exactly as shown and described.</p>

Additional forms of detection are provided by the forms enumerated below, which can be combined with any

<p dir="rtl">15 Number and in what manner are logically and technically consistent.</p>

Additional forms of disclosure are provided by the forms listed below, which may be combined in any number and in any manner that is logically and technically consistent.

Model 1. A method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition comprising a porous support material, palladium, and at least one ionic liquid 20 with a process gas comprising

Ethylene, present in the process gas in an amount of at least 10 mole %;

Acetylene, present in the process gas in an amount of at least 1 ppm;

Hydrogen, present in the process gas in an amount of at least 5 mole %; and

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0 1 ppm to 190 ppm carbon monoxide;

Where at least 90% of the acetylene in the process gas is hydrogenated, and not more than 1% by mole of the total acetylene and ethylene in the process gas is converted to ethane.

<p dir="rtl">5 Model 2. A method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition comprising a porous support material, palladium, and at least one ionic liquid with a process gas comprising</p>

Ethylene, present in the process gas in an amount of at least 10 mole %;

Acetylene, present in the process gas in an amount of at least 1 ppm;

<p dir="rtl">10 Hydrogen, present in the process gas in an amount of at least 5 mole %; and</p>

600 At least 1 ppm of carbon monoxide;

Where at least 90% of the acetylene in the process gas is hydrogenated, and not more than 1% by mole of the total acetylene and ethylene in the process gas is converted to ethane.

<p dir="rtl">15 Model 3. A method according to Model 1 or 2, wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) in the range from 2,000 h-1 to 40,000 h-1.</p>

Model 4. A method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition comprising a porous support material, palladium, and one or more ionic liquids 20 with a process gas comprising

Ethylene, present in the process gas in an amount of at least 10 mole %;

Acetylene, present in the process gas in an amount of at least 1 ppm; and

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Hydrogen, present in the process gas in an amount of at least 5 mole %;

where the process gas is in contact with the catalyst at a gas hourly space velocity (GHSV) based on the total catalyst bed volume (i.e., in a single or multiple layers) of at least 7,100 h-1 (e.g., 7,500 h-1 to 40,000 h-1); and

<p dir="rtl">5 Where at least 90% of the acetylene in the process gas is hydrogenated, and not more than 1% by mole of the total acetylene and ethylene in the process gas is converted to ethane.</p>

Model 5. The method according to claim 4, wherein carbon monoxide is present in the process gas in an amount up to 20,000 ppm, e.g. up to 10,000 ppm, 10 or up to 5,000 ppm, up to 2,500 ppm, up to 1,200 ppm, or up to 1,000 ppm.

Model 6. Method according to claim 4, wherein carbon monoxide is present in the process gas in an amount of up to 100 ppm, up to 500 ppm, up to 1,000 ppm, up to 5,000 ppm, or in the range of 10 parts

<p dir="rtl">15 In the range of 10 ppm to 1,200 ppm, in the range of 10 ppm to 500 ppm, in the range of 50 ppm to 5,000 ppm, in the range of 50 ppm to 1,200 ppm, in the range of 50 ppm to 500 ppm, in the range of 75 ppm to 1,200 ppm, in the range of 75 ppm to 500 ppm.</p>

<p dir="rtl">20 Model 7. A method according to any of Models 1, 3 and 4, wherein carbon monoxide is present in the process gas in an amount up to 190 ppm, e.g., up to 175 ppm, or within the range of 1 ppm to 190 ppm, or within the range of 5 ppm to 190 ppm, or 10 ppm to 190 ppm, or 25 ppm to 190 ppm, or 50 ppm to 190 ppm, or 75 ppm</p>

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To 190 ppm, or 1 ppm to 175 ppm, or 5 ppm to 175 ppm, or 10 ppm to 175 ppm, or 25 ppm to 175 ppm, or 50 ppm to 175 ppm, or 100 ppm to 175 ppm.

<p dir="rtl">5 Model 8. A method according to any of embodiments 1, 3 and 4, wherein carbon monoxide is present in the process gas in an amount of up to 150 ppm, for example, up to 140 ppm, for example, within the range of 1 ppm to 150 ppm, or 5 ppm to 150 ppm, or 10 ppm to 150 ppm, or 25 ppm to 150 ppm, or 50 ppm to 150 ppm, or 75 ppm</p>

<p dir="rtl">10 To 150 ppm, 1 ppm to 140 ppm, 5 ppm to 140 ppm, 10 ppm to 140 ppm, 25 ppm to 140 ppm, 50 ppm to 140 ppm, or 75 ppm to 140 ppm.</p>

Model 9. A method according to any of Models 1, 3 and 4, wherein carbon monoxide is present in the process gas in an amount of up to 125 ppm, for example, up to

<p dir="rtl">15 115 ppm, for example, within the range of 1 ppm to 125 ppm, or 5 ppm.</p>

1 ppm to 125 ppm, 10 ppm to 125 ppm, 25 ppm to 125 ppm, 50 ppm to 125 ppm, 75 ppm to 125 ppm, 1 ppm to 115 ppm, 5 ppm to 115 ppm, 10 ppm to 115 ppm, 25 ppm to 115 ppm

<p dir="rtl">20 Per million, or 50 ppm to 115 ppm, or 75 ppm to 115 ppm.</p>

Model 10. A method according to any of embodiments 1, 3 and 4, wherein carbon monoxide is present in the process gas in an amount up to 110 ppm, for example, up to 100 ppm, for example, within the range of 1 ppm to 110 ppm, or 5 ppm to 110 ppm, or 10 ppm to 110 ppm, or 25 ppm

<p dir="rtl">25 10 ppm to 110 ppm, 50 ppm to 110 ppm, or 75 ppm</p>

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To 110 ppm, or 1 ppm to 100 ppm, or 5 ppm to 100 ppm, or 10 ppm to 100 ppm, or 25 ppm to 100 ppm, or 50 ppm to 100 ppm.

Model 11. Method according to any of Models 1, 3 and 4, wherein carbon monoxide is present

<p dir="rtl">5 monoxide in the process gas in an amount up to 95 ppm, for example, up to 90 ppm, for example, within the range of 1 ppm to 95 ppm, or 5 ppm to 95 ppm, or 10 ppm to 95 ppm, or 25 ppm to 95 ppm, or 50 ppm to 95 ppm, or 1 ppm to 90 ppm, or 5 ppm to 90 ppm, or 10 ppm to 90 ppm</p>

<p dir="rtl">10 Per million, or 25 ppm to 90 ppm, or 50 ppm to 90 ppm.</p>

Model 12. A method according to any of embodiments 1, 3 and 4, wherein carbon monoxide is present in the process gas in an amount up to 85 ppm, for example, up to 80 ppm, for example, within the range of 1 ppm to 85 ppm, or 5 ppm to 85 ppm, or 10 ppm to 85 ppm, or 25 ppm

<p dir="rtl">15 To 85 ppm, or 50 ppm to 85 ppm, or 1 ppm to 80 ppm, or 5 ppm to 80 ppm, or 10 ppm to 80 ppm, or 25 ppm to 80 ppm, or 50 ppm to 80 ppm.</p>

Model 13. A method according to any of embodiments 1-12, wherein carbon monoxide is not added to a feed gas stream to provide a process gas.

<p dir="rtl">20 Model 14. A method according to any of embodiments 2–4, wherein carbon monoxide is present in the process gas in an amount within the range of 600 ppm to 20,000 ppm, or 600 ppm to 15,000 ppm, or 600 ppm to 12,500 ppm, or 700 ppm to 10,000 ppm, or 800 ppm to</p>

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7,500 ppm, or 900 ppm to 5,000 ppm, or 700 ppm to 5,000 ppm, or 800 ppm to 5,000 ppm.

Model 15. A method according to any of embodiments 2-4, wherein carbon monoxide is present in the process gas in an amount within the range of 800 ppm to 20,000 ppm

<p dir="rtl">5 In million, or 800 ppm to 15,000 ppm, or 800 ppm to 10,000 ppm, or 800 ppm to 5,000 ppm, or 800 ppm to 2,500 ppm, or 800 ppm to 1,500 ppm.</p>

Model 16. A method according to any of embodiments 2-4, wherein carbon monoxide is present in the process gas in an amount within the range of 1,000 ppm to 20,000 ppm, or 1,000 ppm to 15,000 ppm, or 1,000 ppm to 10,000 ppm, or 1,000 ppm to 5,000 ppm, or 1,000 ppm to 2,500 ppm.

Model 17. A method according to any of embodiments 2-4, wherein carbon monoxide is present in the process gas in an amount within the range of 1,500 ppm to 20,000 ppm, or 1,500 ppm to 15,000 ppm, or 1,500 ppm to 10,000 ppm, or 1,500 ppm to 5,000 ppm.

Model 18. A method according to any of embodiments 2-4, wherein carbon monoxide is present in the process gas in an amount within the range of 2,000 ppm to 20,000 ppm, or 2,000 ppm to 15,000 ppm, or 2,000 ppm to 20-10,000 ppm, or 2,000 ppm to 5,000 ppm.

Model 19. A method according to any of embodiments 1, 2 and 4–18, wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 7,100 h-1, e.g., within the range 7,100 h-1 to 40,000 h-1, or 7,100 h-1 to 30,000 h-1, or 7,100 h-1 to 20,000 h-1.

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Model 20. A method according to any of embodiments 1, 2 and 4–18, wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 7,500 h-1, e.g., within the range 7,500 h-1 to 40,000 h-1, or 7,500 h-1 to 30,000 h-1, or 7,500 h-1 to 20,000 h-1.

<p dir="rtl">5 Model 21. A method according to any of embodiments 1, 2 and 4–18, wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 10,000 h-1, e.g., within the range of 10,000 h-1 to 40,000 h-1, or 10,000 h-1 to 30,000 h-1, or 10,000 h-1 to 20,000 h-1.</p>

<p dir="rtl">10 Model 22. A method according to any of embodiments 1, 2 and 4–18, wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 12,500 h-1, e.g., within the range of 12,500 h-1 to 40,000 h-1, or 12,500 h-1 to 30,000 h-1, or 12,500 h-1 to 20,000 h-1.</p>

<p dir="rtl">15 Model 23. A method according to any of embodiments 1, 2 and 4–18, wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 15,000 h-1, e.g., within the range of 15,000 h-1 to 40,000 h-1, or 15,000 h-1 to 30,000 h-1, or 15,000 h-1 to 20,000 h-1.</p>

<p dir="rtl">20 Model 24. A method according to any of embodiments 1, 2 and 4–18, wherein the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) of at least 20,000 h-1, e.g., within the range 20,000 h-1 to 40,000 h-1, or 20,000 h-1 to 30,000 h-1.</p>

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Model 25. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at a temperature within the range 20°C to 140°C.

Model 26. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at a temperature within the range 40°C to 100°C.

<p dir="rtl">5 Model 27. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at a temperature within the range 40°C to 90°C.</p>

Model 28. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at a temperature within the range 50°C to 90°C.

Model 29. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at 10°C in the range 50°C to 100°C.

Model 30. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at a temperature within the range of 20°C to 130°C, e.g., within the range of 20°C to 120°C, 20°C to 110°C, 20°C to 100°C, or 20°C to 90°C.

<p dir="rtl">15 Model 31. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at a temperature within the range 40°C to 140°C, e.g., 40°C to 130°C, 40°C to 120°C, or 40°C to 110°C.</p>

Model 32. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at 20°C within the range 50°C to 140°C, e.g., 50°C to 130°C

100°C, or 50°C to 120°C, or 50°C to 110°C.

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Model 33. A method according to any of embodiments 1–24, wherein the selective hydrogenation is carried out at a temperature within the range 60°C to 140°C, e.g., 60°C to 130°C, 60°C to 120°C, 60°C to 110°C, 60°C to 100°C, or 60°C to 90°C.

<p dir="rtl">5 Model 34. A method according to any of embodiments 1–33, wherein at least 95% of the acetylene in the process gas is hydrogenated, e.g., at least 96%, at least 97%, or at least 97.5% of the acetylene in the process gas is hydrogenated.</p>

Model 35. A method according to any of embodiments 1–33, wherein at least 98% of the acetylene in the process gas is hydrogenated, e.g., at least 98.5%, or at least 99% of the acetylene in the process gas is hydrogenated.

Model 36. A method according to any of embodiments 1–33, wherein substantially all of the acetylene present in the process gas is hydrogenated.

Model 37. A method according to any of embodiments 1–36, wherein the amount of ethane in the selective hydrogenation product is not more than 1 mole percent greater than the amount of ethane in the process gas.

<p dir="rtl">15 Model 38. A method according to any of embodiments 1–36, wherein the amount of ethane in the selective hydrogenation product is not more than 0.9 mol %, e.g., not more than 0.8 mol % more than the amount of ethane in the process gas.</p>

Model 39. A method according to any of embodiments 1–36, wherein the amount of ethane in the selective hydrogenation product is not more than 0.7 mol %, e.g., not more than 0.6 mol % more than the amount of ethane 20 in the process gas.

Model 40. A method according to any of embodiments 1–36, wherein the amount of ethane in the selective hydrogenation product is not more than 0.5 mole percent more than the amount of ethane in the process gas.

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Model 41. A method according to any of embodiments 1–36, wherein the amount of ethane in the selective hydrogenation product is not more than 0.2 mol % more than the amount of ethane in the process gas.

Model 42. A method according to any of embodiments 1–36, wherein the amount of ethane in the selective hydrogenation product is not more than 0.1 mol % more than the amount of ethane in the process gas.

<p dir="rtl">5 Model 43. A method according to any of embodiments 1–36, wherein the amount of ethane in the selective hydrogenation product is not more than 0.05 mol% more than the amount of ethane in the process gas.</p>

Model 44. A method according to any of Models 1–44, wherein ethylene is present in the process gas in an amount in the range of 10 mol% to 70 mol%, 15 mol% to 60 mol%, or 15 mol% to 50 mol%.

<p dir="rtl">10 Model 45. A method according to any of embodiments 1–44, wherein ethylene is present in the process gas in an amount of at least 20 mole %, e.g., in the range 20 mole % to 70 mole %, or 20 mole % to 60 mole %, or 20 mole % to 50 mole %.</p>

Model 46. A method according to any of embodiments 1–44, wherein ethylene is present in the process gas in an amount of at least 30 mole %, e.g., in the range 30 mole % to 70 mole %, or 30 15 mole % to 60 mole %, or 30 mole % to 50 mole %.

Model 47. Method according to any of embodiments 1–47, wherein acetylene is present in the gas

Treatment at a quantity of at least 10 parts per million, e.g., at least 50 parts per million.

Model 48. Method according to any of embodiments 1–47, wherein acetylene is present in the gas

Treatment at a quantity of at least 100 ppm, e.g., at least 500 ppm.

<p dir="rtl">20 Model 49. A method according to any of embodiments 1–47, wherein acetylene is present in the process gas in an amount in the range from 10 parts per million to 2 mole percent, e.g., 10 parts per million to 1 mole percent, or 10 parts per million to 0.5 mole percent.</p>

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Model 50. A method according to any of embodiments 1–47, wherein acetylene is present in the process gas in an amount in the range from 50 ppm to 2 mol%, e.g., 50 ppm to 1 mol%, or 50 ppm to 0.5 mol%.

Model 51. A method according to any of embodiments 1–47, wherein acetylene is present in the process gas 5 in an amount in the range from 100 ppm to 2 mol%, e.g., 100 ppm to

<p dir="rtl">1 % per mole, or 100 parts per million to 0.5 % per mole.</p>

Model 52. A method according to any of embodiments 1–47, wherein acetylene is present in the process gas in an amount in the range of 500 ppm to 2 mol%, or 500 ppm to 1 mol%, or 500 ppm to 0.5 mol%.

<p dir="rtl">10 Model 53. A method according to any of embodiments 1–47, wherein acetylene is present in the process gas in an amount of at least 0.1 mol %, e.g., at least 0.5 mol % or at least 1 mol %.</p>

Model 54. A method according to any of embodiments 1–47, wherein acetylene is present in the process gas in an amount in the range from 0.1 mol % to 2 mol %, e.g., 0.5 mol % to 2

<p dir="rtl">15 % per mole, or 1% per mole to 2% per mole, or 0.1% per mole to 1.5% per mole, or 0.5% per mole to 1.5% per mole, or 1% per mole to 1.5% per mole, or 0.1% per mole to 1% per mole, or 0.5% per mole to 1% per mole.</p>

Model 55. A method according to any of embodiments 1–54, wherein hydrogen is present in the process gas in an amount of at least 6 mole %, at least 7 mole %, or at least 8 mole %,

<p dir="rtl">20 Or at least 9% per mole, or at least 10% per mole.</p>

Model 56. A method according to any of embodiments 1–54, wherein hydrogen is present in the process gas in an amount in the range of 5% by mole to 50% by mole, e.g., 5% by mole to 35% by mole, or 5% by mole to 20% by mole, or 5% by mole to 15% by mole, or 8% by mole to 50% by mole, or 8% by mole to 35% by mole, or 8% by mole to 20% by mole, or 8% by mole

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To 15%/mol, or 10%/mol to 50%/mol, or 10%/mol to 35%/mol, or

<p dir="rtl">10 % per mole to 20% per mole, or 10% per mole to 15% per mole.</p>

Model 57. The method according to any of embodiments 1–56, wherein the process gas is provided from a effluent stream of a cracking process, from an overflow stream of a depropanization facility, from an overflow stream of a deethanizer facility, or from a refining facility exhaust gas stream.

Model 58. The method according to any of Models 1–57, wherein the process gas contains not more than

<p dir="rtl">10 % per mole (e.g., more than 5% per mole, more than 2% per mole, or not more than 1% per mole) of compounds containing carbon other than C1 components (e.g., methane, carbon monoxide, carbon dioxide), components</p>

<p dir="rtl">10 C2 (e.g., ethylene, ethane, and acetylene) and C3 components (e.g., propane, propylene, propane, methyl acetylene, and propadiene).</p>

Model 59. The method according to any of Models 1–57, wherein the process gas contains not more than

20 % per mole (eg, greater than 15% per mole, greater than 10% per mole or greater than 5% per mole)

<p dir="rtl">15 % per mole (of carbon-containing compounds other than ethylene, ethane, acetylene, carbon monoxide, carbon dioxide and methane).</p>

Model 60. A method according to any of embodiments 1–59, wherein the catalyst composition comprises a porous support material selected from alumina, silica, titania, and mixtures thereof, present

<p dir="rtl">20 In the catalyst composition in an amount within the range of 90 wt% to 99.9 wt%, e.g., 92.5 wt% to 99.9 wt%, or 95 wt% to 99.9 wt%, or 97.5 wt% to 99.9 wt%.</p>

Model 61. The method according to Model 60, wherein the porous carrier is a porous alumina carrier, e.g., a porous alpha carrier.

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Model 62. A method according to any of embodiments 1–61, wherein the catalyst composition comprises palladium in an amount of at least 0.02 wt%, e.g., within the range 0.02 wt% to 0.5 wt%, or 0.03 wt% to 0.4 wt%, or 0.04 wt% to 0.3 wt%.

Model 63. A method according to any of embodiments 1–62, wherein the catalyst composition comprises at least one ionic liquid 5 in a total amount of up to 10 wt%.

Model 64. A method according to any of embodiments 1-62, wherein the catalyst composition comprises at least one ionic liquid in an amount in the range of 0.5 wt% to 4 wt%, or 0.5 wt% to 3 wt%, or 0.5 wt% to 2 wt%.

Model 65. A method according to any of embodiments 1-64, wherein the thickness of the ionic liquid shell at 10 an outer surface of the catalyst is in the range of 10 to 2000 μm, e.g., 100 to 1000 μm,

Or 100 to 800 micrometers.

Model 66. A method according to any of embodiments 1–65, wherein the at least one ionic liquid is selected from 1-butyl-3-methylimidazolium triflate, 1-ethyl-3-methylpyridinium ethyl sulfate, 1-butyl-1-methylpyrrolidinium triflate, 1-butyl-2,3-dimethylimidazolium triflate, 1

<p dir="rtl">15 Butyl-3-methylimidazolium tricyanomethane, 1-Butyl-3-methylimidazolium methyl sulfate, 1-Butyl-3-methylimidazolium octyl sulfate, 1-Butyl-3-methylimidazolium tetrafluoroborate, 1-Ethyl-3-methylimidazolium ethyl sulfate, 1-Ethyl-3-methylimidazolium methylphosphonate, 1-Ethyl-3-methylimidazolium triflate, 1-Butyl-1-methylpyrrolidinium bis(t)trifluoromethylsulfonyl(imide), 1-Butyl-1-methylpyrrolidinium tetracyanoborate, 1-Butyl-1-methyl</p>

20 Pyrrolidinium tris)pentafluoroethyl(t-trifluorophosphate, 1-butyl-3-methylimidazolium bis)fluoromethylsulfonyl(imide, 1-butyl-3-methylimidazolium tricyanomethane, 1-ethyl-3-methylpyridinium bis)fluoromethylsulfonyl(imide, 1-ethyl-3-methylimidazolium tricyanoborate, 1-ethyl-3-methylimidazolium tris)pentafluoroethyl(t-trifluorophosphate, 1-methyl-3-octylimidazolium triflate, ethyl dimethyl-)2-methoxyethyl(ammonium tris)pentafluoroethyl(t-trifluorophosphate)

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Fluorophosphate, tributylmethylammonium dicyanoamide, tricyclohexyltetradecylphosphonium tris)pentafluoroethyl)trifluorophosphate, and 1-ethyl-3-methylimidazolium bis)trifluoromethylsulfonyl(imide).

Figure 67. Method for starting a selective hydrogenation reactor,

<p dir="rtl">5 The reactor has one or more catalyst beds each containing a catalyst suitable for selectively hydrogenating acetylene in a process gas comprising at least 10 mole % ethylene, at least 1 ppm acetylene, and at least 5 mole % hydrogen, the method comprising</p>

Providing each catalyst layer at not more than a first temperature, the catalyst of the catalyst layer is in contact 10 with a first gas, the first gas being unreactive in the presence of the catalyst at the first temperature;

In the presence of the first gas, heating each catalyst layer to at least a second temperature, the second temperature being at least 20°C higher than the first temperature, the first gas being unreactive in the presence of the catalyst at the second temperature; and then

Changing the composition of the gas in contact with the catalyst from the first gas to the process gas stream while the catalyst layer 15 is at at least the second temperature; and

Allow the process gas to flow through the catalyst bed until the acetylene concentration at the reactor outlet is less than 1 ppm.

20

Model 68. The method according to Model 67, wherein the concentration of acetylene at the reactor outlet is less than 1 ppm during six hours (e.g., during four hours or even during two hours) of the process gas introduced into the one or more catalyst beds.

Model 69. The method according to Model 67 or Model 68, wherein the catalyst of each catalyst bed in the reactor is not in contact with carbon monoxide in an amount exceeding 100 ppm,

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Whereas the method includes refraining from adding carbon monoxide to the process gas.

Model 70. A method for starting a selective hydrogenation reactor, the reactor having one or more catalyst beds each containing a suitable catalyst

<p dir="rtl">5 Selective hydrogenation of acetylene in a process gas containing at least 10 mole % of ethylene</p>

<p dir="rtl">1 , ethylene at least 1 ppm of acetylene, and at least 5 mole % of hydrogen, the method comprising</p>

Providing each catalyst bed at no more than a first temperature, the catalyst bed catalyst is in contact with the process gas;

<p dir="rtl">10 In the presence of the process gas, heating each catalyst layer to at least a second temperature, the second temperature being at least 20°C higher than the first temperature, heating each catalyst layer being carried out at a rate in the range of at least 3°C/hour; and</p>

Allow the process gas to flow through the catalyst bed until the acetylene concentration at the reactor outlet is less than 1 ppm.

<p dir="rtl">15 Form 71. The method according to Form 70, wherein the rate is in the range 3-20°C/h, e.g., 3-15°C/h or 3-12°C/h.</p>

Form 72. Method according to Form 70, where the rate is in the range of 6-20 degrees

Celsius/hour, for example, 6-15°C/hour or 6-12°C/hour.

Form 73. Method according to Form 70, where the rate is in the range of 9-20 degrees

<p dir="rtl">20 Celsius/hour, for example, 9-15°C/hour.</p>

Model 74. A method for starting a selective hydrogenation reactor, the reactor having one or more catalyst beds each containing a catalyst suitable for selectively hydrogenating acetylene in a process gas comprising at least 10 mole percent of ethylene

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<p dir="rtl">1 ,ethylene at least 1 ppm of acetylene, and at least 5 mole % of hydrogen, the method comprising;</p>

Providing the reactor with each catalyst bed having a catalyst in contact with a first gas, the first gas being unreactive in the presence of the catalyst at the first temperature, as the catalyst in the reactor is not in contact with a gas containing

<p dir="rtl">5 On carbon monoxide the concentration of carbon monoxide exceeds 2000 parts per million; and</p>

Introducing the process gas flow into one or more catalyst beds, and refraining from adding carbon monoxide to the process gas.

Model 75. The method according to Model 74, further comprising raising the temperature of the catalyst layer of each catalyst layer 10 from not more than a first temperature to at least a second temperature.

Model 76. The method according to Model 75, wherein the temperature of the catalyst bed is raised prior to introducing the process gas.

Model 77. The method according to claim 75, wherein the temperature of the catalyst bed is raised after introduction of the process gas.

<p dir="rtl">15 Model 78. The method according to claim 75, wherein the process gas is introduced while the temperature of the catalyst bed is raised.</p>

Embodiment 79. The method according to any of Embodiments 75-78 further includes, after raising the temperature to at least the second temperature, flowing the process gas through the one or more catalyst beds until the reactor effluent has less than 1 ppm (e.g., less than 0.5 ppm

<p dir="rtl">20 From (acetylene).</p>

Model 80. The method according to any of Models 67-79, wherein the initial temperature does not exceed 50°C, e.g., in the range 31-50°C or 35-50°C, or 40-50°C, or 45-50°C.

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Model 81. The method according to any of Models 67-79, wherein the initial temperature does not exceed 45°C, e.g., in the range 31-45°C, 35-45°C, or 40-45°C.

Model 82. The method according to any of Models 67-79, wherein the initial temperature does not exceed 40.5°C, e.g., in the range 31-40°C or 35-40°C.

Form 83. The method according to any of Forms 67-79, wherein the initial temperature does not exceed 30°C, or does not exceed 25°C.

Model 84. A method for starting a selective hydrogenation reactor, the reactor having one or more catalyst beds each containing a suitable catalyst 10 for selectively hydrogenating acetylene in a process gas comprising at least 10 mole percent of ethylene

<p dir="rtl">1 , ethylene at least 1 ppm of acetylene, and at least 5 mole % of hydrogen, the method comprising</p>

Dry one or more layers of catalyst at a temperature of at least 50°C; then

<p dir="rtl">15 Cool each dried catalyst layer to a first temperature in the range of 31-50°C, and contact the catalyst of each catalyst with the process gas at the first temperature; then</p>

In the presence of the process gas, heating each catalyst layer to at least a second temperature, the second temperature being at least 20 degrees higher than the first temperature; and

Allow the process gas to flow through the catalyst bed until the acetylene concentration at the reactor outlet is less than 1 ppm.

Form 85. Method according to Form 84, wherein the first temperature is within the range 35°C to 50°C, e.g., 40°C to 50°C, or 45°C to 50°C.

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Form 86. Method according to Form 84, wherein the first temperature is within the range 31°C to 45°C, e.g., 35°C to 45°C, or 40°C to 45°C.

Model 87. Method according to Model 84, wherein the initial temperature is within the range 31°5C to 40°C, e.g., 35°C to 40°C.

Model 88. Method according to any of Models 67-87, wherein the second temperature is within the range 40°C to 140°C.

Model 89. Method according to any of Models 67-87, wherein the second temperature is within the range 40°C to 100°C.

<p dir="rtl">10 Model 90. Method according to any of Models 67-87, wherein the second temperature is within the range 40°C to 90°C.</p>

Model 91. Method according to any of Models 67-87, wherein the second temperature is within the range 50°C to 90°C.

Model 92. Method according to any of the models v, wherein the second temperature is within the range 50 15°C to 100°C.

Model 93. A method according to any of Models 67-87, wherein the second temperature is within the range 20°C to 130°C, e.g., within the range 20°C to 120°C, or 20°C to 110°C, or 20°C to 100°C, or 20°C to 90°C.

<p dir="rtl">20 Model 94. A method according to any of Models 67-87, wherein the second temperature is within the range 40°C to 140°C, e.g., 40°C to 130°C, or 40°C to 120°C, or 40°C to 110°C.</p>

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Model 95. A method according to any of Models 67-87, wherein the second temperature is within the range 50°C to 140°C, e.g., 50°C to 130°C, or 50°C to 120°C, or 50°C to 110°C.

Model 96. Method according to any of Models 67-87, wherein the second temperature is within the range

<p dir="rtl">5 From 60°C to 140°C, for example, 60°C to 130°C, or 60°C to 120°C, or 60°C to 110°C, or 60°C to 100°C, or 60°C to 90°C.</p>

Model 97. A method according to any of Models 67-96, wherein the second temperature is at least 30°C greater (e.g., at least 40°C greater) than the first temperature.

<p dir="rtl">10 Model 98. A method according to any of Models 67-96, wherein the second temperature is at least 50°C greater (e.g., at least 60°C greater) than the first temperature.</p>

Model 99. The method according to any of Models 67-98, wherein the temperature of each catalyst layer is raised from not more than the first temperature to at least the second temperature over a period of time not more than 10 hours, e.g., not more than six hours.

<p dir="rtl">15 Model 100. Method according to any of Models 67-69, 74-83 and 88-99, wherein the first gas contains not more than 1 ppm of acetylene (e.g., not more than 0.5 ppm).</p>

Model 101. A method according to any of Models 67-100, wherein the process gas comprises at least 10 parts per million of carbon monoxide (CO).

<p dir="rtl">20 Model 102. A method according to any of Embodiments 67-100, wherein the process gas is otherwise as described in respect of one or more of Embodiments 1-66.</p>

Form 103. Method according to any of Forms 67-69, 74-83 and 88-102, wherein each

Catalyst layer from first gas contact to process gas contact within a time period not exceeding 10

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Hours, for example, not more than six hours, for example, in the range of 2-10 hours, 4-10 hours, or 3-6 hours.

Model 104. The method according to any of Models 67-104, wherein the catalyst is as described in one or more of Models 1-66

<p dir="rtl">5 Model 105. A method according to any of embodiments 1-104, further comprising, prior to introducing the process gas into the bed or contacting the catalyst composition with the process gas, reducing the catalyst (e.g., with a gas flow containing hydrogen).</p>

Figure 106. Hydrogenation catalyst composition comprising:

A porous carrier material, present in the composition in an amount within the range of 90% by weight to 99.9% by weight;

<p dir="rtl">10 Palladium, present in the composition in an amount within the range of 0.02 wt% to 0.5 wt% (e.g., within the range of 0.03 wt% to 0.4 wt%, or 0.04 wt% to 0.3 wt%), calculated on an elemental mass basis; and</p>

One or more ionic liquids, present in the composition in a combined amount of up to 10% by weight.

Model 107. The catalyst composition according to Model 106, wherein palladium is present in the composition.

<p dir="rtl">15 In an amount within the range of 0.02 wt% to 0.5 wt%, e.g., 0.02 wt% to 0.4 wt%, or 0.02 wt% to 0.3 wt%, or 0.02 wt% to 0.2 wt%, or 0.02 wt% to 0.15 wt%.</p>

Model 108. The catalyst composition according to Model 106, wherein palladium is present in the composition in an amount within the range of 0.04 wt% to 0.5 wt%, e.g., 0.04 wt%20 to 0.4 wt%, or 0.04 wt% to 0.3 wt%, or 0.04 wt% to 0.2 wt%, or 0.04 wt% to 0.15 wt%.

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Model 109. The catalyst composition according to Model 106, wherein palladium is present in the composition in an amount within the range of 0.05 wt% to 0.5 wt%, e.g., 0.05 wt% to 0.4 wt%, 0.05 wt% to 0.3 wt%, 0.05 wt% to 0.2 wt%, or 0.05 wt% to 0.15 wt%.

<p dir="rtl">5 Model 110. The catalyst composition according to Model 106, wherein palladium is present in the composition in an amount within the range of 0.06 wt% to 0.5 wt%, e.g., 0.06 wt% to 0.4 wt%, 0.06 wt% to 0.3 wt%, 0.06 wt% to 0.2 wt%, or 0.06 wt% to 0.15 wt%.</p>

Model 111. The catalyst composition according to Model 106, wherein palladium is present in composition 10 in an amount within the range of 0.08 wt% to 0.5 wt%, e.g., 0.08 wt% to 0.4 wt%, 0.08 wt% to 0.3 wt%, 0.07 wt% to 0.2 wt%, or 0.07 wt% to 0.15 wt%.

Figure 112. Hydrogenation catalyst composition comprising:

A porous carrier, present in the composition in an amount within the range of 90 wt% to 99.9 wt%, 15 having a BET surface area of ​​not more than 10 m2/g and a pore volume of at least 0.1 mL/g;

Palladium, present in the composition in an amount within the range of at least 0.02% by weight, calculated on the basis of elemental mass; and

One or more ionic liquids, present in the composition in a combined amount of up to 10% by weight.

Model 113. Hydrogenation catalyst according to Model 112, comprising palladium in an amount of at least 0.03% by weight, at least 0.04% by weight, at least 0.05% by weight, or

At least 0.06% by weight, or at least 0.07% by weight, or at least 0.08% by weight, or at least 0.09% by weight, or at least 0.1% by weight, or at least 0.11% by weight, or

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At least 0.12% by weight, at least 0.13% by weight, at least 0.14% by weight, or at least 0.15% by weight.

Model 114. The hydrogenation catalyst according to Model 112, comprising palladium in an amount of not more than 0.5% by weight (e.g., not more than 0.4% by weight, not more than 0.3% by weight, or not more than 0.2% by weight).

Model 115. The hydrogenation catalyst according to Model 112, comprising palladium in an amount within the range of 0.02 wt% to 0.5 wt%, 0.02 wt% to 0.45 wt%, 0.03 wt% to 0.4 wt%, 0.03 wt% to 0.35 wt%, 0.04 wt% to 0.3 wt%, or 0.04 wt% to 0.25 wt%.

<p dir="rtl">10 Embodiment 116. A catalyst composition according to any of Embodiments 106-115, further comprising at least one promoter (e.g., silver, gold, zinc, tin, lead, gallium, cadmium, copper, bismuth, sodium, cesium, or potassium), present in the composition in an amount within the range of 0.05 wt% to 0.25 wt%, e.g., 0.08 wt% to 0.25 wt%, or 0.1 wt% to 0.25 wt%, calculated on an elemental mass basis.</p>

<p dir="rtl">15 Embodiment 117. Hydrogenation catalyst according to any of Embodiments 106-116, wherein the porous carrier material has a BET surface area in the range of 2 m2/g to 10 m2/g.</p>

Embodiment 118. Hydrogenation catalyst According to any of the embodiments 106-116, the porous carrier material has a BET surface area within the range of 2 m2/g to 9 m2/g, or 2 m2/g to 8 m2/g, or 2 m2/g to 7 m2/g, or 2 m2/g to 6 m2/g, or 2 m2/g to 5 m2/g, or 3 m2/g to 20 10 m2/g, or 4 m2/g to 10 m2/g, or 5 m2/g to 10 m2/g, or 6 m2/g to 10

m2/g, or 2 m2/g to 6 m2/g, or 3 m2/g to 7 m2/g, or 4 m2/g to 8 m2/g, or 5 m2/g to 9 m2/g.

Embodiment 119. Hydrogenation catalyst according to any of Embodiments 106-118, wherein the porous carrier has a pore volume within the range of 0.10 mL/g to 1.0 mL/g.

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Model 120. Hydrogenation catalyst according to any of 106-118, wherein the porous carrier has a pore size within the range of 0.10 mL/g to 0.80 mL/g, or 0.20 mL/g to 0.80 mL/g, or 0.30 mL/g to 0.80 mL/g, or 0.20 mL/g to 0.70 mL/g, or 0.30 mL/g to 0.70 mL/g.

<p dir="rtl">5 Figure 121. Hydrogenation catalyst composition comprising:</p>

A porous carrier material, present in the composition in an amount within the range of 90% by weight to 99.9% by weight;

Palladium, present in the composition in an amount within the range of at least 0.02% by weight, calculated on the basis of elemental mass; and

One or more ionic liquids, present in the composition in a combined amount of up to 10% by weight,

<p dir="rtl">10 Where the hydrogenation catalyst has a BET surface area of ​​not more than 10 m2/g and a pore volume of at least 0.05 mL/g.</p>

Model 122. The hydrogenation catalyst according to Model 121, comprising palladium in an amount of at least 0.03 wt%, at least 0.04 wt%, at least 0.05 wt%, at least 0.06 wt%, at least 0.07 wt%, at least 0.08 wt%, at least 0.09 wt%, at least 0.1 wt%, at least 0.11 wt%, or

At least 0.12% by weight, at least 0.13% by weight, at least 0.14% by weight, or at least 0.15% by weight.

Model 123. Hydrogenation catalyst of Model 121 or Model 122, comprising palladium in an amount of not more than 0.5% by weight (e.g., not more than 0.4% by weight, not more than 20% by weight, not more than 0.3% by weight, or not more than 0.2% by weight).

Model 124. The hydrogenation catalyst according to Model 121, comprising palladium in an amount within the range of 0.02 wt% to 0.5 wt%, or 0.02 wt% to 0.45 wt%, or 0.03

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%by weight to 0.4%by weight, or 0.03%by weight to 0.35%by weight, or 0.04%by weight to 0.3%by weight, or 0.04%by weight to 0.25%by weight.

Embodiment 125. The hydrogenation catalyst according to any of Embodiments 121-124, further comprising at least one promoter (e.g., silver, gold, zinc, tin, lead, gallium, cadmium, copper, bismuth, sodium, cesium, or potassium), present in the composition in an amount within the range of 0.05 wt% to 0.25 wt%, e.g., 0.08 wt% to 0.25 wt%, or 0.1 wt% to 0.25 wt%, calculated on an elemental mass basis.

Model 126. The hydrogenation catalyst according to any of embodiments 121-125, having a BET surface area in the range from 2 m2/g to 10 m2/g.

<p dir="rtl">10 Embodiment 127. The hydrogenation catalyst according to any of Embodiments 121-125, having a BET surface area within the range of 2 m2/g to 9 m2/g, or 2 m2/g to 8 m2/g, or 2 m2/g to 7 m2/g, or 2 m2/g to 6 m2/g, or 2 m2/g to 5 m2/g, or 3 m2/g to 10 m2/g, or 4 m2/g to 10 m2/g, or 5 m2/g to 10 m2/g, or 6 m2/g to 10 m2/g, or 2 m2/g to 6 m2/g, or 3 m2/g to 7 m2/g, or 4 m2/g to 8 m2/g, or 5 m2/g to 9 m2/g.</p>

<p dir="rtl">15 Embodiment 128. The hydrogenation catalyst according to any of Embodiments 121-127, having a pore size within the range of 0.05 mL/g to 1.0 mL/g.</p>

Embodiment 129. The hydrogenation catalyst according to any of Embodiments 121-127, having a pore size within the range of 0.05 mL/g to 0.4 mL/g.

Embodiment 130. The hydrogenation catalyst according to any of Embodiments 121-129, having a pore size within the range of 20 0.10 mL/g to 1.0 mL/g, e.g., 0.10 mL/g to 0.80 mL/g, or

0.10 to 0.60 mL/g, 0.10 to 0.40 mL/g, or 0.10 to 0.30 mL/g.

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Embodiment 131. The hydrogenation catalyst according to any of embodiments 121-129, having a pore size within the range of 0.20 mL/g to 1.0 mL/g, e.g., 0.20 mL/g to 0.80 mL/g, or 0.20 to 0.60 mL/g, or 0.20 to 0.40 mL/g, or 0.20 to 0.35 mL/g.

<p dir="rtl">5 Embodiment 132. The hydrogenation catalyst according to any of Embodiments 121-129, having a pore size within the range of 0.40 mL/g to 1.0 mL/g, e.g., 0.40 mL/g to 0.80 mL/g, or 0.40 to 0.60 mL/g.</p>

Embodiment 133. is a hydrogenation catalyst according to any of Embodiments 121-132, wherein the difference between the pore volume of the support and the pore volume of the catalyst (i.e., including palladium, i.e., the booster 10 and the ionic liquid) is in the range of 10-90% of the pore volume of the support.

Embodiment 134. is a hydrogenation catalyst according to any of Embodiments 121-132, wherein the difference between the pore volume of the support and the pore volume of the catalyst (i.e., including palladium, i.e., the booster and the ionic liquid) is in the range of 10-80% of the pore volume of the support, e.g., 20-80%, 30-80%, or 40-80% of the pore volume of the support.

<p dir="rtl">15 Embodiment 135. is a hydrogenation catalyst according to any of Embodiments 121-132, wherein the difference between the pore volume of the support and the pore volume of the catalyst (i.e., including palladium, i.e., the booster and the ionic liquid) is in the range of 10-70% of the pore volume of the support, e.g., 20-70%, 30-70%, or 40-70%; or in the range of 10-60% of the pore volume of the support, e.g., 20-60%, 30-60%, or 40-60%.</p>

<p dir="rtl">20 Model 136. The hydrogenation catalyst according to any of claims 106-135, wherein the ionic liquid is present in an amount in the range from 0.1 wt% to 10 wt%, e.g., 0.1 wt% to 8 wt%, 0.1 wt% to 6 wt%, 0.1 wt% to 4 wt%, 0.1 wt% to 3 wt%, 0.1 wt% to 2 wt%, or 0.1 wt% to 1 wt%.</p>

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Embodiment 137. The hydrogenation catalyst according to any of Embodiments 106-135, wherein the ionic liquid is present in an amount in the range of 0.2 to 3 wt%.

Embodiment 138. Hydrogenation catalyst according to any of Embodiments 106-135, wherein the ionic liquid is present in an amount in the range of 0.5 to 4 wt%.

<p dir="rtl">5 Model 139. Hydrogenation catalyst according to any of Models 106-138, containing silver as a promoter.</p>

Model 140. Hydrogenation catalyst according to any of embodiments 106-139, wherein the porous carrier is a porous alumina carrier, e.g., a porous alpha alumina carrier.

Embodiment 141. Hydrogenation catalyst according to any of Embodiments 106-140, wherein the thickness of the ionic liquid shell at an external surface of the catalyst is in the range of 10 to 2000 micrometers, e.g., 100 to

<p dir="rtl">10 1000 micrometers, or 100 to 800 micrometers.</p>

Embodiment 142. Hydrogenation catalyst according to any of Embodiments 106-138, wherein the at least one ionic liquid is selected from 1-butyl-3-methylimidazolium triflate, 1-ethyl-3-methylpyridinium ethyl sulfate, 1-butyl-1-methylpyrrolidinium triflate, 1-butyl-2,3-dimethylimidazolium triflate, 1-butyl-3-methylimidazolium taricyanomethane, 1-butyl-3-methylimidazolium

<p dir="rtl">15 Methyl sulfate, 1-butyl-3-methylimidazolium octyl sulfate, 1-butyl-3-methylimidazolium tetrafluoroborate, 1-ethyl-3-methylimidazolium ethyl sulfate, 1-ethyl-3-methylimidazolium methylphosphonate, 1-ethyl-3-methylimidazolium triflate, 1-butyl-1-methylpyrrolidinium bis)t-trifluoromethylsulfonyl(imide), 1-butyl-1-methylpyrrolidinium tetrafluoroborate, 1-butyl-1-methylpyrrolidinium tris)pentafluoroethyl(t-trifluorophosphate, 1-butyl-3-methyl</p>

20 Imidazolium bis(t)fluoromethylsulfonyl(imide), 1-butyl-3-methylimidazolium tricyanomethane, 1-ethyl-3-methylpyridinium bis(t)fluoromethylsulfonyl(imide), 1-ethyl-3-methylimidazolium tricyanoborate, 1-ethyl-3-methylimidazolium tris)pentafluoroethyl(t)fluorophosphate, 1-methyl-3-octylimidazolium triflate, ethyl dimethyl-)2-methoxyethyl(ammonium tris)pentafluoroethyl(t)fluorophosphate, tributylmethylammonium dicyanoamide, tricyclo

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Hexyltetradecylphosphonium tris)pentafluoroethyl)trifluorophosphate, and 1-ethyl-3-methylimidazolium bis)trifluoromethylsulfonyl(imide).

Model 143. Any of the operations of Models 1–59 and 67–105, using the catalyst as described in any of Models 106–142.

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