High solids slurry polymerization

<u>BACKGROUND OF THE INVENTION</u>

This invention relates to the polymerization of olefin monomers in a liquid diluent.

Addition polymerizations are frequently carried out in a liquid which is a solvent for the resulting polymer. When high density (linear) ethylene polymers first became commercially available in the 1950's this was the method used. It was soon discovered that a more efficient way to produce such polymers was to carry out the polymerization under slurry conditions. More specifically, the polymerization technique of choice became continuous slurry polymerization in a pipe loop reactor with the product being taken off by means of settling legs which operated on a batch principle to recover product. This technique has enjoyed international success with billions of pounds of ethylene polymers being so produced annually. With this success has come the desirability of building a smaller number of large reactors as opposed to a larger number of small reactors for a given plant capacity.

Settling legs, however, do present two problems. First, they represent the imposition of a "batch" technique onto a basic continuous process. Each time a settling leg reaches the stage where it "dumps" or "fires" accumulated polymer slurry it causes an interference with the flow of slurry in the loop reactor upstream and the recovery system downstream. Also the valve mechanism essential to periodically seal off the settling legs from the reactor upstream and the recovery system downstream requires frequent maintenance due to the difficulty in maintaining a tight seal with the large diameter valves needed for sealing the legs.

Secondly, as reactors have gotten larger, logistic problems are presented by the settling legs. If a pipe diameter is doubled the volume of the reactor goes up four-fold. However, because of the valve mechanisms involved, the size of the settling legs cannot easily be increased further. Hence the number of legs required begins to exceed the physical space available.

In spite of these limitations, settling legs have continued to be employed where olefin polymers are formed as a slurry in a liquid diluent. This is because, unlike bulk slurry polymerizations (i.e. where the monomer is the diluent) where solids concentrations of better than 60 percent are routinely obtained, olefin polymer slurries in a diluent are generally limited to no more than 37 to 40 weight percent solids. Hence settling legs have been believed to be necessary to give a final slurry product at the exit to the settling legs of greater than 37-40 percent. This is because, as the name implies, settling occurs in the legs to thus increase the solids concentration of the slurry finally recovered as product slurry.

Another factor affecting maximum practical reactor solids is circulation velocity, with a higher velocity for a given reactor diameter allowing for higher solids since a limiting factor in the operation is reactor fouling due to polymer build up in the reactor.

<patcit id="pcit0001" dnum="EP0432555A"><text>EP-A 0 432 555</text></patcit> discloses a polymerization process, wherein the volume solids concentration of the polymerization reaction slurry is optimized using a specific control system. This reference is silent on how the product is withdrawn from the reactor.

<patcit id="pcit0002" dnum="US4613484A"><text>US-A 4 613 484</text></patcit> relates to an apparatus for separating solid polymer particles from a polymerization slurry mixture using a settling leg. Likewise, <patcit id="pcit0003" dnum="EP0415427A"><text>EP-A 0 415 427</text></patcit> relates to a polymer recovery process using a settling leg.

<u>SUMMARY OF THE INVENTION</u>

It is an object of this invention to produce olefin polymers as a slurry in a liquid diluent utilizing continuous product slurry takeoff;

It is a further object of this invention to operate a slurry olefin polymerization process in a diluent at a reactor solids concentration high enough to make direct continuous product takeoff commercially viable;

It is a further object of this invention to operate a slurry olefin polymerization process in a diluent at higher circulation velocities.

It is yet a further object of this invention to operate a slurry olefin polymerization process in a diluent in a reaction zone of greater than 113.6 m³ (30,000 gallons); and

It is still yet a further object of this invention to provide a loop reactor apparatus having a capacity of greater than 113.6 m³ (30,000 gallons) and having a continuous take off means.

In accordance with one aspect of this invention, an olefin polymerization process is carried out at a higher reactor solids concentration by means of continuous withdrawal of product slurry.

In accordance with another aspect of this invention, a loop reactor olefin polymerization process is carried out by operating at a higher circulation velocity for a given reactor pipe diameter.

In accordance with another aspect of this invention, a loop polymerization apparatus is provided having an elongated hollow appendage at a downstream end of one of the longitudinal segments of the loop, the hollow appendage being in direct fluid communication with a heated flash line and thus being adapted for continuous removal of product slurry.

<u>BRIEF DESCRIPTION OF THE DRAWINGS</u>

In the drawings, forming a part hereof, <figref idref="f0001">Fig. 1</figref> is a schematic perspective view of a loop reactor and polymer recovery system; <figref idref="f0002">Fig. 2</figref> is a cross section along line 2-2 of <figref idref="f0001">Fig. 1</figref> showing a continuous take off appendage; <figref idref="f0002">Fig. 3</figref> is a cross section along line 3-3 of <figref idref="f0002">Fig 2</figref> showing a ram valve arrangement in the continuous take off assembly; <figref idref="f0003">Fig. 4</figref> is a cross section of a tangential location for the continuous take off assembly; <figref idref="f0003">Fig. 5</figref> is a side view of an elbow of the loop reactor showing both a settling leg and continuous take off assemblies; <figref idref="f0003">Fig. 6</figref> is a cross section across line 6-6 of <figref idref="f0003">Fig. 5</figref> showing the orientation of two of the continuous take off assemblies; <figref idref="f0004">Fig. 7</figref> is a side view showing another orientation for the continuous take off assembly; <figref idref="f0004">Fig. 8</figref> is a cross sectional view of the impeller mechanism; <figref idref="f0005">Fig. 9</figref> is a schematic view showing another configuration for the loops wherein the upper segments 14a are 180 degree half circles and wherein the vertical segments are at least twice as long as the horizontal segments and <figref idref="f0005">Fig. 10</figref> is a schematic view showing the longer axis disposed horizontally.

<u>DETAILED DESCRIPTION OF THE INVENTION</u>

Surprisingly, it has been found that continuous take off of product slurry in an olefin polymerization reaction carried out in a loop reactor in the presence of an inert diluent allows operation of the reactor at a much higher solids concentration. Commercial production of predominantly ethylene polymers in isobutane diluent has generally been limited to a maximum solids concentration in the reactor of 37-40 weight percent. However, the continuous take off has been found to allow significant increases in solids concentration. Furthermore, the continuous take off itself brings about some additional increase in solids content as compared with the content in the reactor from which it takes off product because of the placement of the continuous take off appendage which selectively removes a slurry from a stratum where the solids are more concentrated.

Throughout this application, the weight of catalyst is disregarded since the productivity, particularly with chromium oxide on silica, is extremely high.

Also surprisingly, it has been found that more aggressive circulation (with its attendant higher solids concentration) can be employed. Indeed more aggressive circulation in combination with the continuous take off, solids concentrations of greater than 50 weight percent can be removed from the reactor by the continuous take off. For instance, the continuous take off can easily allow operating at 5-6 percentage points higher; i.e., the reactor can be adjusted to easily raise solids by 10 percent; and the more aggressive circulation can easily add another 7-9 percentage points which puts the reactor above 50 percent. But, because the continuous take off is positioned to take off slurry from a stratum in the stream which has a higher than average concentration of solids, the product actually recovered has about 3 percentage points (or greater) higher concentration than the reactor slurry average. Thus the operation can approach an effective slurry concentration of 55 weight percent or more, i.e. 52 percent average in the reactor and the removal of a component which is actually 55 percent (i.e. 3 percentage points) higher.

It must be emphasized that in a commercial operation as little as a one percentage point increase in solids concentration is of major significance. Therefore going from 37-40 average percent solids concentration in the reactor to even 41 is important; thus going to greater than 50 is truly remarkable.

The present invention is applicable to olefin polymerization in a loop reactor utilizing a diluent so as to produce a product slurry of polymer and diluent. The invention is suitable for the homopolymerization of ethylene and the copolymerization of ethylene and butene, 1-pentene, 1-hexene, 1-octene or 1-decene. Especially preferred is ethylene and 0.01 to 10, preferably 0.01 to 5, most preferably 0.1 to 4 weight percent higher olefin based on the total weight of ethylene and comonomer. Alternatively sufficient comonomer can be used to give the above-described amounts of comonomer incorporation in the polymer.

Suitable diluents (as opposed to solvents or monomers) are well known in the art and include hydrocarbons which are inert and liquid under reaction conditions. Suitable hydrocarbons include isobutane, propane, n-pentane, i-pentane, neopentane and n-hexane, with isobutane being especially preferred.

Suitable catalysts are well known in the art. Particularly suitable is chromium oxide on a support such as silica as broadly disclosed, for instance, in <patcit id="pcit0004" dnum="US2285721A"><text>Hogan and Banks, US 2,285,721 (March 1958</text></patcit>) , the disclosure of which is hereby incorporated by reference.

Referring now to the drawings, there is shown in <figref idref="f0001">Fig. 1</figref> a loop reactor <b>10</b> having vertical segments <b>12</b>, upper horizontal segments <b>14</b> and lower horizontal segments <b>16</b>. These upper and lower horizontal segments define upper and lower zones of horizontal flow. The reactor is cooled by means of two pipe heat exchangers formed by pipe <b>12</b> and jacket <b>18</b>. Each segment is connected to the next segment by a smooth bend or elbow <b>20</b> thus providing a continuous flow path substantially free from internal obstructions. The polymerization mixture is circulated by means of impeller <b>22</b> (shown in <figref idref="f0004">Fig. 8</figref>) driven by motor <b>24</b>. Monomer, comonomer, if any, and make up diluent are introduced via lines <b>26</b> and <b>28</b> respectively which can enter the reactor directly at one or a plurality of locations or can combine with condensed diluent recycle line <b>30</b> as shown. Catalyst is introduced via catalyst introduction means <b>32</b> which provides a zone (location) for catalyst introduction. The elongated hollow appendage for continuously taking off an intermediate product slurry is designated broadly by reference character <b>34</b>. Continuous take off mechanism <b>34</b> is located in or adjacent to a downstream end of one of the lower horizontal reactor loop sections <b>16</b> and adjacent or on a connecting elbow <b>20</b>.

The continuous take off appendage is shown at the downstream end of a lower horizontal segment of the loop reactor which is the preferred location. The location is in an area near the last point in the loop where flow turns upward before the catalyst introduction point so as to allow fresh catalyst the maximum possible time in the reactor before it first passes a take off point.

Also, the segment of the reactor to which the continuous take off appendage is attached can be of larger diameter to slow down the flow and hence further allow stratification of the flow so that the product coming off can have an even greater concentration of solids.

The continuously withdrawn intermediate product slurry is passed via conduit <b>36</b> into a high pressure flash chamber <b>38</b>. Conduit <b>36</b> includes a surrounding conduit <b>40</b> which is provided with a heated fluid which provides indirect heating to the slurry material in flash line conduit <b>36</b>. Vaporized diluent exits the flash chamber <b>38</b> via conduit <b>42</b> for further processing which includes condensation by simple heat exchange using recycle condenser <b>50</b>, and return to the system, without the necessity for compression, via recycle diluent line <b>30</b>. Recycle condenser <b>50</b> can utilize any suitable heat exchange fluid known in the art under any conditions known in the art. The temperature range for this fluid is 4 to 54°C (40 degrees F to 130 degrees F). Polymer particles are withdrawn from high pressure flash chamber <b>38</b> via line <b>44</b> for further processing using techniques known in the art. Preferably they are passed to low pressure flash chamber <b>46</b> and thereafter recovered as polymer product via line <b>48</b>. Separated diluent passes through compressor <b>47</b> to line <b>42</b>. This high pressure flash design is broadly disclosed in <patcit id="pcit0005" dnum="US4424341A"><text>Hanson and Sherk, US 4,424,341 (Jan. 3, 1984</text></patcit>), the disclosure of which is hereby incorporated by reference. Surprisingly, it has been found that the continuous take off not only allows for higher solids concentration upstream in the reactor, but also allows better operation of the high pressure flash, thus allowing the majority of the withdrawn diluent to be flashed off and recycled with no compression. Indeed, 70 to 90 percent of the diluent can generally be recovered in this manner. This is because of several factors. First of all, because the flow is continuous instead of intermittent, the flash line heaters work better. Also, the pressure drop after the proportional control valve that regulates the rate of continuous flow out of the reactor has a lower pressure which means when it flashes it drops the temperature lower thus further giving more efficient use of the flash line heaters.

Referring now to <figref idref="f0002">Fig. 2</figref>, there is shown elbow <b>20</b> with continuous take off mechanism <b>34</b> in greater detail. The continuous take off mechanism comprises a take off cylinder <b>52</b>, a slurry withdrawal line <b>54</b>, an emergency shut off valve <b>55</b>, a proportional motor valve <b>58</b> to regulate flow and a flush line <b>60</b>. The reactor is run "liquid" full. Because of dissolved monomer the liquid has slight compressibility, thus allowing pressure control of the liquid full system with a valve. Diluent input is generally held constant, the proportional motor valve <b>58</b> being used to control the rate of continuous withdrawal to maintain the total reactor pressure within designated set points.

Referring now to <figref idref="f0002">Fig. 3</figref>, which is taken along section line 3-3 of <figref idref="f0002">Fig. 2</figref>, there is shown the smooth curve or elbow <b>20</b> having associated therewith the continuous take off mechanism <b>34</b> in greater detail, the elbow <b>20</b> thus being an appendage-carrying elbow. As shown, the mechanism comprises a take off cylinder <b>52</b> attached, in this instance, at a right angle to a tangent to the outer surface of the elbow. Coming off cylinder <b>52</b> is slurry withdrawal line <b>54</b>. Disposed within the take off cylinder <b>52</b> is a ram valve <b>62</b> which serves two purposes. First it provides a simple and reliable clean-out mechanism for the take off cylinder if it should ever become fouled with polymer. Second, it can serve as a simple and reliable shut-off valve for the entire continuous take off assembly.

<figref idref="f0003">Figure 4</figref> shows a preferred attachment orientation for the take off cylinder <b>52</b> wherein it is affixed tangentially to the curvature of elbow <b>20</b> and at a point just prior to the slurry flow turning upward. This opening is elliptical to the inside surface. Further enlargement could be done to improve solids take off.

<figref idref="f0003">Figure 5</figref> shows four things. First, it shows an angled orientation of the take off cylinder <b>52</b>. The take off cylinder is shown at an angle, alpha, to a plane that is (1) perpendicular to the centerline of the horizontal segment <b>16</b> and (2) located at the downstream end of the horizontal segment <b>16</b>. The angle with this plane is taken in the downstream direction from the plane. The apex for the angle is the center point of the elbow radius as shown in <figref idref="f0003">Fig. 5</figref>. The plane can be described as the horizontal segment cross sectional plane. Here the angle depicted is about 24 degrees. Second, it shows a plurality of continuous take off appendages, <b>34</b> and <b>34a</b>. Third, it shows one appendage, <b>34</b> oriented on a vertical center line plane of lower segment <b>16</b>, and the other, <b>34a</b>, located at an angle to such a plane as will be shown in more detail in <figref idref="f0003">Fig. 6</figref>. Finally, it shows the combination of continuous take off appendages <b>34</b> and a conventional settling leg <b>64</b> for batch removal, if desired.

As can be seen from the relative sizes, the continuous take off cylinders are much smaller than the conventional settling legs. Yet three 50.8-mm (2-inch) ID continuous take off appendages can remove as much product slurry as 14 203-mm (8-inch) ID settling legs. This is significant because with current large commercial loop reactors of 56.8-68.2 m³ (15,000-18000 gallon) capacity, six 203 mm (eight inch) settling legs are required. It is not desirable to increase the size of the settling legs because of the difficulty of making reliable valves for larger diameters. As noted previously, doubling the diameter of the pipe increases the volume four-fold and there simply is not enough room for four times as many settling legs to be easily positioned. Hence the invention makes feasible the operation of larger, more efficient reactors. Reactors of 113.6 m³ (30,000 gallons) or greater are made possible by this invention. Generally the continuous take off cylinders will have a nominal internal diameter within the range of 25.4 mm (1 inch) to less than 203 mm (8 inches). Preferably they will be about 50.8-76.2 mm (2-3 inches) internal diameter.

<figref idref="f0003">Figure 6</figref> is taken along section line 6-6 of <figref idref="f0003">Fig. 5</figref> and shows take off cylinder <b>34a</b> attached at a place that is oriented at an angle, beta, to a vertical plane containing the center line of the reactor. This plane can be referred to as the vertical center plane of the reactor. This angle can be taken from either side of the plane or from both sides if it is not zero. The apex of the angle is located at the reactor center line. The angle is contained in a plane perpendicular to the reactor center line as shown in <figref idref="f0003">Fig. 6</figref>.

It is noted that there are three orientation concepts here. First is the attachment orientation, i.e. tangential as in <figref idref="f0003">Fig. 4</figref> and perpendicular as in <figref idref="f0002">Fig. 2</figref> or <figref idref="f0004">7</figref> or any angle between these two limits of 0 and 90 degrees. Second is the orientation relative to how far up the curve of the elbow the attachment is as represented by angle alpha ( <figref idref="f0003">Fig. 5</figref>). This can be anything from 0 to 60 degrees but is preferably 0 to 40 degrees, more preferably 0 to 20 degrees. Third is the angle, beta, from the center plane of the longitudinal segment (<figref idref="f0003">Fig. 6</figref>). This angle can be from 0 to 60 degrees, preferably 0 to 45 degrees, more preferably 0-20 degrees.

<figref idref="f0004">Fig. 7</figref> shows an embodiment where the continuous take off cylinder <b>52</b> has an attachment orientation of perpendicular, an alpha orientation of 0 (inherent since it is at the end, but still on, the straight section), and a beta orientation of 0, i.e. it is right on the vertical centerline plane of the lower horizontal segment <b>16</b>.

<figref idref="f0004">Fig. 8</figref> shows in detail the impeller means <b>22</b> for continuously moving the slurry along its flow path. As can be seen in this embodiment the impeller is in a slightly enlarged section of pipe which serves as the propulsion zone for the circulating reactants. Preferably the system is operated so as to generate a pressure differential of at least 0.124 MPa gauge (18 psig) preferably at least 0.138 MPa gauge (20 psig), more preferably at least 0.152 MPa gauge (22 psig) between the upstream and downstream ends of the propulsion zone in a nominal 61 cm (two foot) diameter reactor with total flow path length of about 290 m (950 feet) using isobutane to make predominantly ethylene polymers. As much as 0.345 MPa gauge (50 psig) or more is possible. This can be done by controlling the speed of rotation of the impeller, reducing the clearance between the impeller and the inside wall of the pump housing or by using a more aggressive impeller design as is known in the art. This higher pressure differential can also be produced by the use of at least one additional pump.

Generally the system is operated so as to generate a pressure differential, expressed as a loss of pressure per unit length of reactor, of at least 0.23 (0.07), generally 0.23 to 0.49 mm (0.07 to 0.15 foot) pressure drop per mm (foot) of reactor length for a nominal 610 mm (24 inch) diameter reactor. Preferably, this pressure drop per unit length is 0.29 to 0.36 (0.09 to 0.11) for a 610 mm (24 inch) diameter reactor. For larger diameters, a higher slurry velocity and a higher pressure drop per unit length of reactor is needed. This assumes the density of the slurry which generally is about 0.5 - 0.6 g/cm³.

Referring now to <figref idref="f0005">Fig. 9</figref> the upper segments are shown as 180 degree half circles which is the preferred configuration. The vertical segments are at least twice the length, generally about seven to eight times the length of the horizontal segments. For instance, the vertical flow path can be 57.9-68.6 m (190 - 225 feet) and the horizontal segments 7.6-9.1 m (25 - 30 feet) in flow path length. Any number of loops can be employed in addition to the four depicted here and the eight depicted in <figref idref="f0001">Fig. 1</figref>, but generally four or six are used. Reference to nominal 61 cm (two foot) diameter means an internal diameter of about 6.68 m (21.9 inches). Flow length is generally greater than 152 m (500 feet), generally greater than 274 m (900 feet), with about 287 to 411 m (940 to 1,350 feet) being quite satisfactory.

Commercial pumps for utilities such as circulating the reactants in a closed loop reactor are routinely tested by their manufacturers and the necessary pressures to avoid cavitation are easily and routinely determined.

<u>EXAMPLES</u>

A four vertical leg polymerization reactor using a 660 mm (26 inch) Lawrence Pumps Inc. pump impeller D51795/81-281 in a M51879/FAB casing was used to polymerize ethylene and hexene-1. This pump was compared with a 610 mm (24 inch) pump which gave less aggressive circulation 20.1 cm (0.66 ft of pressure drop vs 29.9 cm (0.98)). This was then compared with the same more aggressive circulation and a continuous take off assembly of the type shown by reference character 34 of <figref idref="f0003">Fig. 5</figref>. The results are shown below. <tables id="tabl0001" num="0001"><table frame="all"><tgroup cols="4"><colspec colnum="1" colname="col1" colwidth="77mm" /><colspec colnum="2" colname="col2" colwidth="30mm" /><colspec colnum="3" colname="col3" colwidth="30mm" /><colspec colnum="4" colname="col4" colwidth="30mm" /><thead valign="top"><row><entry namest="col1" nameend="col4" align="center"><b>DATA TABLE</b></entry></row><row><entry align="center"><b>Description</b></entry><entry align="center"><b>24 in Pump</b></entry><entry align="center"><b>26 in Pump</b></entry><entry align="center"><b>26 in Pump + CTO</b></entry></row></thead><tbody><row><entry>Date of Operation</entry><entry align="center">Oct 4-9, 1994</entry><entry align="center">May 24-28, 1995</entry><entry align="center">Nov 15-18, 1996</entry></row><row><entry>Avg. Reactor Solids Concentration, wt %</entry><entry align="center">39</entry><entry align="center">45</entry><entry align="center">53</entry></row><row><entry>Polymer Production Rate, (mlbs/hr) g/h</entry><entry align="center">(40.1) 18.2</entry><entry align="center">(40.7) 18.5</entry><entry align="center">(39.9) 18.1</entry></row><row><entry>Reactor Circulation Pump Power, kw</entry><entry align="center">430</entry><entry align="center">691</entry><entry align="center">753</entry></row><row><entry>Circulation Pump Pressure Diff, (psi) kPa</entry><entry align="center">(14.3) 98.7</entry><entry align="center">(22.4) 154.6</entry><entry align="center">(23.7) 163.5</entry></row><row><entry>Circulation Pump Head, (ft) m</entry><entry align="center">(61.8) 18.8</entry><entry align="center">(92.5) 28.2</entry><entry align="center">(92.4) 28.2</entry></row><row><entry>Reactor Slurry Flow Rate, mGPM</entry><entry align="center">39</entry><entry align="center">46</entry><entry align="center">45</entry></row><row><entry>Reactor Slurry Density, g/cm³</entry><entry align="center">0.534</entry><entry align="center">0.558</entry><entry align="center">0.592</entry></row><row><entry>Reactor Temperature, °C (F)</entry><entry align="center">(215.6) 102.0</entry><entry align="center">(218.3) 103.5</entry><entry align="center">(217.0) 102.8</entry></row><row><entry>Ethylene Concentration, wt %</entry><entry align="center">4.43</entry><entry align="center">3.67</entry><entry align="center">4.9</entry></row><row><entry>Hexene-1 Concentration, wt %</entry><entry align="center">0.22</entry><entry align="center">0.17</entry><entry align="center">0.14</entry></row><row><entry>Reactor Heat Transfer Coefficient</entry><entry align="center">270</entry><entry align="center">262</entry><entry align="center">241</entry></row><row><entry>Reactor Inside Diameter, (inches) mm</entry><entry align="center">(22.0625) 560.388</entry><entry align="center">(22.0625) 560.388</entry><entry align="center">(22.0625) 560.388</entry></row><row><entry>Reactor Volume, (gal) m³</entry><entry align="center">(18700) 70.81</entry><entry align="center">(18700) 70.81</entry><entry align="center">(18700) 70.81</entry></row><row><entry>Reactor Length, (ft) m</entry><entry align="center">(941) 287</entry><entry align="center">(941) 287</entry><entry align="center">(941) 287</entry></row><row><entry>Pressure Drop per mm (Foot) of Reactor, (ft/ft) mm/mm</entry><entry align="center">(0.066) 0.217</entry><entry align="center">(0.098) 0.322</entry><entry align="center">(0.098) 0.322</entry></row></tbody></tgroup></table></tables>

While this invention has been described in detail for the purpose of illustration, it is not to be construed as limited thereby, but is intended to cover all changes within the spirit and scope thereof.