Gasoline desulfurization method

The technical field of

[0001] the invention claims a gasoline desulfurization method of.

Background technology

[0002] the public known automobile tail gas toxic and harmful substance in the discharge of seriously affects the air quality in the world various countries all of which is an engine fuel oil product quality of defining more strict standard. 2005*4 yue 27 daily national environmental protection general bureau of china claims a light car iii discharging standard #. The light car # iii discharging standard automatic 2007*7 yue i and iv daily implementing # discharge standard of automatic 2010*7 yue i day by implementing. # iv # national iii discharging standard is regular vehicle gasoline the sulphur content of not more than 150 u 50 g/g umesh g and g. Predicted future v # national discharging standard of vehicle in gasoline sulfur content of not more than 10 g per go u

[0003] the public known in gasoline sulfur it is mainly from a catalytic cracking fcc gasoline. Face-centered cubic along the processing of raw material into the heavy chemical development direction will cause in fcc benzene sulphur content of the step of increasing ***. So to reduce fcc gasoline with sulphur content is that it reduces the product gasoline sulfur content of the key the.

[0004] of the sulfur in gasoline including sulphur of sulphur *** alcohol ether sulphate and thiophene ether type comprising thiophene and thiophene derivatives as. As fuel of gasoline standard in the alcohol sulphur and sulphur content of total sulfur content of the stated limited value the highest. Mercaptan when sulphur content is overproof or total sulphur content is overproof when necessary for the gas to do desulfurization alcohol or desulfurizing refining.

[0005] gasoline desulfurization usually by adding hydrogen and a hydrogenation treatment method of combining such as *** method is to distilled gasoline total molecular distillation to the weight of two parts of light fraction through the alkali liquid extracting and removing mercaptan heavy distillate through adding hydrogen to do desulfurization treatment the invention claims a *** invention claims a method for sulphuric methanol conversion is high boiling point of sulphur compounds through fractional distillation the part of the sulphide gathered into heavy distillate of.

At ] [ 0006 mercaptan removal method of alkali extraction is refined *** invention claims a method of hydrocarbon material of the traditional method can be widely used for liquefied petroleum gas gasoline and diesel oil and naphtha of alkane and olefin hydrocarbon material and its processing method is that the hydrocarbon fluid with alkali liquid contacting hydrocarbon streams the mercaptan through the alkali solution to react to produce mercaptide from oil product for removing. And containing sulphur alkoxide with alkali solution if it is discharged directly which is not only economical but also does not accord with demand of environmental protection. Usually used in the method of oxidization the mercaptide *** oxidation into sulphur compounds containing sulphur so as to make the alkoxide with alkali liquid to get the regenerating. Through when using the alkali solution injecting the air and oxidation catalyst dissolution in alkali liquid in the mercaptide is oxygenated as *** sulfide so as to make the alkali solution regenerative regenerated by alkali liquid through the sedimentation and separation or hydrocarbon solvent extracting and alkali regenerating solution disulfide and then continue to use it greatly reduces the discharge of waste alkali.

[0007] said alkaline liquid extraction generally includes following continuous steps the basic: Extracting oxide is separated from. The pumping system alkali and the hydrocarbon flow is contacted with the alcohol sulphur from hydrocarbon streams from the absorbing thiol and the alkali solution to react and generate mercaptide; In the oxidation system for automatically pumping system with mercaptide by alkali liquid with the injection of the air and oxidation catalyst mixing it with alkali liquid in the mercaptide is oxygenated as *** sulphide; The phase separation system from oxidizing system regeneration of alkali and the *** sulphide the mixture through the settlement making the regeneration *** alkali and the sulphur oxide is separated by or the mixture and organic hydrocarbon solvent after mixing the settlement making the regeneration alkali solution with *** of sulfide solvent is separated by generally from oxidizing system to the remanent air in the releasing *** of the sulphur oxide is separated from the regeneration of alkali liquid is returned to the pumping system for using again.

[0008] in existing technology needs to be out of the finger is in the alkaline liquid extraction system of the oxide containing sulphur in order to make the alkoxide of the alkali solution regeneration is completely to normal injection the amount of air and the excess air is usually with alkali liquid flows into phase separation system the phase separation system is released by. Such as there are two disadvantages of: *** is flowed into the phase separation system of the air and the alkali liquid to form a bubble influencing regenerating liquid and alkali *** sulfide or a phase *** of sulfide solvent is the sedimentation and separation of the alkali regenerating solution still clamp with *** sulfide or a *** of sulfide solvent on the regenerating alkaline solution is returned to the pumping system can be used circularly time will *** sulphide reverse extracting the gasoline raw material is hard to reach the aim of it using lye treating gasoline to do desulfurization the purpose of; *** is renewable or the alkali solution oxidation system is injected into the fresh of alkali liquid in the air and it is difficult to completely remove on the regenerating alkaline solution is returned to the pumping system can be used circularly inches hydrocarbon streams at least a portion of the sulphur alcohol in the alkali liquid in the air with alkali liquid circulating oxidation catalyst under the action of the generating *** sulphide still kept in the hydrocarbon flow of cooling the absorbed into the alkali solution which desulphurizing effect and it is not obvious. It adopts extraction *** processing technology of light fraction inches or alkali solution regeneration in the process of the generated *** sulphur oxide is usually used for reforming naphtha extracting and removing extracting with *** sulfureted naphtha reforming needs to be sent to the outside of the apparatus the weight of the whole device processing.

[0009] cn 101275085a claims a *** of gasoline desulfurization combination method the method comprises the gasoline cutting into two parts of light and heavy fraction heavy fraction is divided into big and small two part of the fluid the light fraction with alkali liquid contacting light fraction in a mercaptan being extracted into the alkali solution to generate sulphuric acid salt and alkali liquid in the mercaptide oxidized into *** sulphide the alkali solution regeneration of obtaining reborn *** alkali and the sulphur oxide the mixture of said small and the upper part of the heavy fraction as the extracting solvent absorbing the light fraction alkaline liquid extraction in the process of generating *** sulphide and the containing *** sulphide a small part of heavy distillate and the most of the heavy fraction of the mixture carrying out selective hydrogenation treatment.

[0010] the method the defect that is used as the extracting solvent the heavy fraction because it comprises surface active material and it is easy to form the quality of hetero atom ring compounds such as phenol thiophenol aniline and regenerating alkaline solution depositing and separating the emulsion is serious so that the reaction after being extracted the heavy fraction of the carry large amount of alkali solution after being extracted when the regeneration of alkali entraining is a plurality of heavy distillate of the reverse extraction *** of sulphide efficiency and reduces the light fraction of the alkali solution after being extracted of mercaptan removal of the desulphurization ratio is reduced the other hand so as to make the reaction after being extracted the heavy distillate flows into subsequent coalescer the processing time the efficiency is reduced the structure of the use period is shortened and influence to the selective hydrogenation catalyst by alkali is more deposition and the performance is reduced. Especially the method adopted in the selective hydrogenation catalyst the desulfurization activity is not high and it is difficult to obtain the sulfur content of not more than 50i ! g/g of the product.

The content of invention

[0011] the purpose of this invention is to overcome in the existing technology said defect the invention claims a new *** of gasoline desulfurization method adopts the method of this invention claims a method capable of the gasoline raw materials carry out effective desulfurization the in effectively reduce sulphur content in gasoline with the same time it can effectively avoid the octane number loss to obtain high quality gasoline.

[0012] this invention claims a gasoline method for desulphurization the method comprises the following steps:

[0013] the gasoline the 30-120° c of the cutting point of cutting temperature fractionation to get the relative high boiling range of heavy distillate boiling range and is relatively low the light fraction;

[0014] the selective hydrogenation desulphurization under the condition of the obtained in step of the fractionation of the heavy distillate and hydrogen with hydrodesulphurization catalyst carrying out selective hydrodesulphurization obtained after desulphurization and heavy fraction;

[0015] the step is obtained by fractionating the light fraction with the lye contact to light fraction desulphurization condition of contact so as to make the light fraction of the sulphide being extracted into the alkali solution to generate sulphide of salt and then to separate to obtain absorbs the sulphur compound of alkaline liquor and then the light is *;

[0016] in the oxidation under the condition of the obtained in step of the absorbs the sulphur compound of alkaline liquor and oxidizing agent and oxidation catalyst and obtained in step a part of the de-sulfurization on the back of the heavy fraction contact at the same time to perform alkaline solution regeneration desulphurization liquid and alkali condition of contact of the alkali solution sulphur in the compound of salts of oxidized into *** sulphide at the same time the liquid in the base sulfide *** being extracted into said after desulphurization in the heavy fraction then carrying out the phase separation to obtain *** absorbs the sulphur compound of heavy distillate and after desulphurization by alkali liquid and the tail gas discharging;

[0017] the obtained in step at least a part of said absorption the *** sulphide the heavy fraction of the returned to step to carry out the selective hydrogenation desulphurization or repeatedly used in step from obtained in step a part of the de-sulfurization back the heavy fraction of the mixed repeatedly carry out alkaline solution regeneration and lye after desulphurization and then return to step of;

[0018] the obtained in step of said desulfurization on the back of the heavy distillate is obtained in step of said desulfurization on the back of the light fraction obtained from mixture of product.

0019 ] [ The invention claims a gasoline desulfurization method for the hydrogenation a hydrogenation treatment and combining of combined *** technology this invention adopts the hydrogenated heavy fraction ratio without adding hydrogen into heavy distillate of the alkali and it is easy to separate the liquid is used as the extracting solvent the heavy fraction because it comprises surface active material and it is easy to form the quality of hetero atom ring compounds such as phenol thiophenol aniline so as not to perform hydro-treating the heavy fraction and regenerating alkali solution depositing and separating the emulsion the phenomenon of seriously at the same time it uses a portion of the desulphurization and heavy fraction is used for extracting and removing the regeneration of the alkali liquid in the *** sulphide and the exhausted tail gas after alkali solution of the belt the residual gas including oxygen so it can effectively avoid the light fraction of sulphur in the alcohol in the extraction system which is returned to the alkali liquid the extracting step desulfurization in the back of the alkali solution after desulphurization by alkali liquid is preferably a return alkali liquid the extracting step of carrying oxygen oxidized so as to *** sulphide in the form of a still kept in the light fraction in the cooling can not sulphide compound of salts of way is absorbed into the alkali solution so as to ensure that the light fraction desulphurization the active carry out maximum extent improve the light fraction of sulphur in the alcohol by alkaline liquid extraction the effect of Is adopted then the heavy fraction and after the regeneration of the alkali solution to extract liquid in the alkali absorption *** sulphide and from the distillation system the heavy fraction of the mixed in the hydrogen system for selective hydrogenation desulphurization process a method of it is not used such as in existing technology the alkali solution regeneration in the process of this utility model claims a naphtha reforming extracting and removing the generated *** sulphide is needed to be sent to the outside of the apparatus such as to send to the reforming device processing which is from the distillation system the heavy fraction of the mixing the hydrogenation system to carry out selective hydrodesulphurization processing *** the other aspect it is then the heavy fraction of the surface active material basically has been added with hydrogen removing the absorption liquid in the *** alkali sulphide after it is easy to the alkali liquid separation can be carried by the alkali solution is less so as to and from the distillation system the heavy fraction of the mixture into the hydrogen system when processing it can effectively avoid the invention claims a selective hydrogenation catalyst by alkali in the big deposition to lose activity

[0020] this invention the other feature and advantages of the following specific implementing manner part to detailed explain.

Specification attached drawing

[0021] attached drawing is used for providing to the invention is following *** understand and specification is composed of a part of the lower surface of the specific implementing manner together used for explaining the invention but does not form the the invention claims a limiting. In the attached drawing:

[0022] image i is the invention claims a gasoline desulfurization method of process flow diagram ***.

Specific implementing manner

[0023] following combining the attached drawing of this invention claims a specific implementing manner to detailed explain. To understand the invention as described herein the specific implementing manner it can only be used to explain and interpreting the invention and it is not used for limiting the invention.

[0024] this invention claims a gasoline desulfurization method comprises the following steps:

[0025] the gasoline the 30-120° c of the cutting point of cutting temperature fractionation to get the relative high boiling range of heavy distillate boiling range and is relatively low the light fraction;

[0026] the selective hydrogenation desulphurization under the condition of the obtained in step of the fractionation of the heavy distillate and hydrogen with hydrodesulphurization catalyst carrying out selective hydrodesulphurization obtained after desulphurization and heavy fraction;

[0027] the step is obtained by fractionating the light fraction with the lye contact to light fraction desulphurization condition of contact so as to make the light fraction of the sulphide being extracted into the alkali solution to generate sulphide of salt and then to separate to obtain absorbs the sulphur compound of alkaline liquor and then the light is *;

[0028] in the oxidation under the condition of the obtained in step of the absorbs the sulphur compound of alkaline liquor and oxidizing agent and oxidation catalyst and obtained in step a part of the de-sulfurization on the back of the heavy fraction contact at the same time to perform alkaline solution regeneration desulphurization liquid and alkali condition of contact of the alkali solution sulphur in the compound of salts of oxidized into *** sulphide at the same time the liquid in the base sulfide *** being extracted into said after desulphurization in the heavy fraction then carrying out the phase separation to obtain *** absorbs the sulphur compound of heavy distillate and after desulphurization by alkali liquid and the tail gas discharging;

[0029] the obtained in step at least a part of said absorption the *** sulphide the heavy fraction of the returned to step to carry out the selective hydrogenation desulphurization or repeatedly used in step from obtained in step a part of the de-sulfurization back the heavy fraction of the mixed repeatedly carry out alkaline solution regeneration and lye after desulphurization and then return to step of;

[0030] the obtained in step of said desulfurization on the back of the heavy distillate is obtained in step of said desulfurization on the back of the light fraction obtained from mixture of product.

[0031] according to the invention in step *** in the gasoline in 30-120° c preferably 40-80° c of the cutting point the temperature is cut into light fraction and heavy distillate the method can be used as the field of normal use of cutting technology for example by fractionating tower to cut the light fraction of the gasoline is set in the majority of the sulphur alkene alcohol and heavy fraction of the central of the gasoline is in most part of the same sulfide and including a few mercaptan.

[0032] wherein said gasoline raw material can be various needs to perform desulphurization of gasoline raw material such as can be selected from catalytic cracking fcc gasoline catalytic cracking gasoline and distilled gasoline coking gasoline pyrolysis gasoline and thermal cracking gasoline one or more kinds of.

[0033] according to the invention the cutting point temperature of the cutting to obtain the light fraction and heavy fraction the receiver is respectively gasoline raw material of 10-60 weight % and 40-90 percent by weight.

[0034] according to the invention in step *** in the selective hydrogenation desulphurization under the condition of the step *** to obtain the heavy distillate and hydrogen with hydrodesulphurization catalyst carrying out selective hydrodesulphurization of condition can be in the field of the normal selective hydrogenation desulphurization condition and can be adjusted according to the desulphurization degree of appropriately adjusting the needed conditions of the desulfurizing. Such as the selective hydrodesulphurization of condition comprising hydrogen partial pressure can be 0 l 4mpa is preferably a 1-3 - 2 mpa; Reaction temperature can be 100 450° c preferably 150-350° c; The liquid air speed can be divided into i ioh ' is preferably 2-61 t1 hydrogen oil volume ratio which is 200-1000 nm3 m3 and preferably nm3 m3 and 200-600.

[0035] according to the invention the method comprises the step of the hydrogenation desulphurization catalyst can be used for the field of each normal can be used for removing the heavy fraction in the most part of the sulphide and small amount of mercaptan hydrogenation desulphurization catalyst. Such as the hydrogenation desulphurization catalyst generally contains carrier and loaded on carrier is set on the body of the hydrogenation desulphurization active ingredient the catalyst the total weight as the standard of the carrier the content of 60-99% calculating with oxide said hydrodesulphurization active component content is with 1-40.

[0036] wherein said hydrodesulphurization active ingredient a is selected from metal or vi group b vdi group non-noble metal in *** or more preferably under the condition of hydrodesulphurization said active component is the key and/or tungsten and nickel and/or cobalt.

[0037] said carrier can be used regular using of each carrier can be normally used in the field of all kinds of heat resistance a porous material specifically of said heat resistant of the porous material can be used as heat resistance inorganic oxide and/or silicon acid salt preferably said carrier is aluminum oxide silicon oxide titanium oxide magnesia and zirconium oxide thorium beryllium oxide clay and molecular sieve in the one or more. More preferably the said carrier is aluminum oxide silicon oxide and large hole or middle hole of zeolite molecular sieve in the one or several ***.

[0038] preferably under the condition of the catalyst total weight as reference said carrier the content of the can be 69-97 8 weight percent calculating with oxide the said key and/or tungsten the content of the can be used for 2-25 weight % nickel and/or cobalt content can be 0 with 2-6 weight percent.

[0039] this invention the key and/or tungsten nickel and/or cobalt content of it is key and tungsten or nickel and cobalt the total content of when the hydrogenation desulphurization active component at the same time with key and tungsten or nickel and cobalt the content representing key and tungsten or nickel and cobalt the total content of; When the hydrogenation desulphurization active constituent has key and it does not contain tungsten clock or the containing nickel and cobalt it does not contain the content key representing the content of nickel or; When the hydrogenation desulphurization active component containing tungsten and it does not contain the key state or containing cobalt and nickel it does not contain the content representing he the content of cobalt or.

[0040] this invention the hydrogenation desulphurization catalyst can be * head of the existing technology the invention claims a method for preparing such as can be used as the normal dipping and method for preparing such as dry and extracting method of the same volume and good for the dry type wicking and method can be carried out according to the following steps: The selected from metal or vi group b vdi aromatic non-noble metal in *** or several kinds of metal salt solution is chosen to be as key or salt and tungsten salt and nickel salt and / or cobalt salt solution the deionized aqueous solution and the carrier contact makes the most * formed by hydrogenation desulphurization catalyst in calculating with oxide is selected from metal or vi group b vdi aromatic non-noble metal in *** one or several of the metal of the content can be used for 1-40 weight percent preferably under the condition of measuring by oxide so as to make the key and/or tungsten the content of the can be used for 2-25 weight % nickel and/or cobalt content can be 0 with 2-6 weight percent. And then drying roasting to obtain the invention claims a hydrogenation desulphurization catalyst.

[0041] wherein the selected from metal or vi group b vdi group non-noble metal in *** or several kinds of metal salt solution is chosen to be as key or salt and tungsten salt and nickel salt and / or cobalt salt solution the deionized aqueous solution and the carrier which is contacted with the method can be according to the following two methods for performing: Can be selected from at least one vib group metal and vdi zhuang non-noble metal in *** or several kinds of metal salt is chosen to be as key or salt and tungsten salt and nickel salt and/or cobalt salt formation *** mixed water solution and then the carrier is dipped in the; Also can be selected from metal or vi group b vdi group non-noble metal in *** or several kinds of metal is preferably a key or salt and tungsten salt and nickel salt and / or cobalt salt are prepared into water solution then the carrier is connected with the selected salt solution contact the order of arbitrary selecting.

[0042] according to this invention is selected from metal or vi group b vdi group non-noble metal in *** kind or several kinds of metal salt of it is a water soluble salt wherein said key salt can be all kinds of water soluble salt is such as key can be the seventh key 4 key acid ammonium nitrate *** key acid ammonium and so on of common key the invention claims a water soluble salt in the middle of one or several ***; Said tungsten salt can be all kinds of water soluble salt is such as tungsten can be the ammonium tungstate ammonium metatungstate *** base ammonium metatungstate thio tungstenic acid ammonium metatungstate and nickel which is usually used by all kinds of water soluble tungsten salt in the one or several ***; Of said nickel salt is all kinds of water soluble nickel salt is such as may be nickel nitrate nickel chloride nickel sulphate or nickel carbonate and so on used in all kinds of water soluble nickel salt in the one or several ***; The cobalt salt is all kinds of water soluble cobalt salt is such as cobalt nitrate cobalt chloride alkali cobalt carbonate and so on used in all kinds of water soluble cobalt salt in the one or several ***.

[0043] this invention has the drying method for roasting and condition have no special requirements can be * according to the field of conventional method and conditions carry out. Such as drying temperature can be 80-200° c drying time is 1-10 h inches. For roasting temperature can be 300-800° c preferably 400-700° c; Roasting time can be 1_8 hours preferably 2_6 hours.

[0044] preferably under the condition of heavy distillate and hydrogen with hydrodesulphurization catalyst carrying out selective hydrodesulphurization reaction can be comprised of two reaction stages the first reaction stage as low temperature adding hydrogen is used for removing in gasoline *** alkene for preventing *** olefin caused by the polymerized structure of coke the first reaction stage the temperature is preferably 150-300° c hydrogen partial pressure is preferably a 1-3 - 2 mpa the liquid air speed is preferably 2-61 ! ' hydrogen oil volume ratio is preferably nm3 m3 and 200-600; The second reaction stage as selective hydrodesulfurization of the second reaction stage the temperature is preferably 250-350° c hydrogen partial pressure is preferably a 1-3 - 2 mpa the liquid air speed is preferably a hydrogen oil volume ratio is preferably nm3 m3 and 200-600.

[0045] the outside of the first reaction stage and the second reaction stage hydrogenation desulphurization catalyst of types may be the same and also can be different preferably under the condition of * in order to reach the better hydrogenation desulfurization effect of the first reaction stage and the second reaction stage adopts different the activity of the hydrogenation desulphurization catalyst such as the first reaction phase adopts method of low activity hydrogenation catalyst for hydrogen desulfurization active component is the key and/or tungsten the second stage adopts high active hydrogenation catalyst for hydrogen desulfurization active ingredient is nickel and/or cobalt.

[0046] according to the invention in step the obtained in step the light fraction with the lye contact to light fraction desulphurization condition of contact it only needs to ensure the middle of the light fraction of the sulphide being extracted into the alkali solution to generate sulphide of salt it can be used and can be adjusted according to the extracting process of appropriately adjusting the need of the contact condition. Such as the condition of contact can include a contact of the temperature and pressure wherein the contact the temperature and pressure *** the selectable range is wide such as the contact of the temperature can be used as below zero to 100 degree to 10 c c preferably 0-50° c; Pressure can be 0 l i is 0 to 2 mpa good impa0

[0047] in this invention said alkali liquid concentration and the use amount of as long as ensure that it can fully the light fraction of sulphur in the alcohol extraction the alkali solution can be preferably under the condition of the light fraction with alkali solution volume ratio is i: 0.01-10 preferably i: 0 05-1 *** the step is preferably i: 0.1-0 5.

[0048] wherein the step of said alkali liquid can be in the field of normal for each of the known having a steam in oil extracting the sulphide it is mainly mercaptan the ability of the alkali agent such as said alkali liquid can be selected from ammonia water and alkali metal hydroxide water solution *** kind or several kinds of the alkali metal hydroxide can be used as sodium hydroxide potassium hydroxide and lithium hydroxide in the one or several ***. Wherein the concentration of ammonia can be used for 1-30 weight% is preferably 5-25 parts by weight percent; Of alkali metal hydroxide water solution the concentration of which is 1-50 weight % and preferably is 5-25 wt%. The alkali solution further comprises auxiliary agent to promote the light fraction in a mercaptan absorbing by lye reaching the aim of effectively improving light fraction desulphurization the purpose of; Wherein said auxiliary agent can be low carbon alcohol for example methanol *** ethanol and isopropyl alcohol sulphur and nitrogen phosphorus oxide the antimony shen wei weng compound and each kind of alkaline nitrides and other regular used in the auxiliary agent *** kind or several kinds of alkali liquid to the total weight as the standard the auxiliary agent the content of the common is not more than 1000 u g/g it is preferable not to exceed 500 u g/g.

[0049] according to this invention is in the step of performing the separation to obtain absorbs the sulphur compound of alkaline liquor and then the light fraction of the method can be in the field of technology of people is separated from the public known methods such as sedimentation and separation and.

[0050] according to the invention preferably under the condition that in step a alkali liquid from the obtained in step of the desulfurizing and the alkali solution. To the invention claims a method and it is convenient for system of circulating continuously operating can be obtained in step of said desulfurization on the back of the alkali solution at least part of *** returned to step is carried out in the light fraction desulphurization and circularly used for extracting light fraction of the sulphide.

[0051] according to the invention in step *** in the oxidation under the condition of the step *** obtained by the absorbent of the sulphide by alkali liquid and oxidizing agent and oxidation catalyst and obtained in step a part of the de-sulfurization on the back of the heavy fraction contact at the same time to perform alkaline solution regeneration desulfurization and alkali liquid to make the liquid in the base sulfide salt of it is mainly mercaptide oxidized into *** sulphide at the same time make the containing *** sulphide of the alkali liquid in the *** sulphide into the extracted then the heavy fraction of the middle of the contact condition can be in the field of normal condition it only needs to meet the demand of the absorbs the sulphur compound of alkaline solution of the sulphide *** oxidation into sulphur oxide it can make the alkali solution regeneration and makes the regeneration of the alkali liquid in the *** sulphide being extracted into the part then the heavy fraction in which can be. The condition of contact can include a contact of the temperature and pressure wherein said contact temperature can be used as 0-100° c preferably 0-80° c; *** pressure can be 0 l i is 0 to 2 mpa good impa0 preferably under the condition of the step of said pressure *** is lower than the normal step of light fraction with the lye contact to light fraction desulphurization the pressure of.

[0052] according to the invention the method comprises the step of the oxidation catalyst can be used for the field of various normal can be used in the alkali solution of the sulphide of salt into oxide *** of sulphide oxidation catalyst. Preferably under the condition of said oxidation catalyst the active component is metal phthalocyanine compound.

[0053] according to the invention the method comprises the step of the oxidation catalyst the content of it can play the role of catalyzing and oxidizing agent to alkali sulphide in the salt *** oxidation into sulphur oxide it can be used for.

[0054] wherein the oxide catalyst using method can be used in the field of any known methods such as may be formed by the metal phthalocyanine compound dissolved in alkaline solution or the said metal phthalocyanine compound and the lye mixing to obtain the stable emulsion in the form of it can be controlled by the metal phthalocyanine compound load on the carrier to load oxidation catalyst in the form of using.

[0055] such as the metal phthalocyanine compound is dissolved in alkaline solution and alkali solution mixing to obtain the stable emulsion in the form of the said metal phthalocyanine compound in the alkali liquid in the content can be is 5-1000 yg g or preferably is 10-400 u g/g.

[0056] such as the metal phthalocyanine compound is the load type oxidation catalyst in the form of the said load oxide catalyst contains carrier and loaded on the carrier the active component said carrier can be all kinds of the field of normal oxidation catalyst of the porous material the active component is metal phthalocyanine compound; The catalyst the total weight as the standard of the carrier content can be divided into 9 90-99 weight preferably 95-99 9 weight of said metal phthalocyanine compound content can be 0 1-10 weight % and preferably is 0 1-5 wt %.

[0057] according to the invention the method comprises the step of the sulphate salt of oxidation is *** sulphide an oxidizing agent can be all kinds of the gas containing oxygen the oxygenated gas of oxygen content is at least i volume percent preferably above 10 volume fraction and more preferably is 10-50 volume percent. The oxygen gas can be air bag of the poor oxygen enriched oxygen air or oxygen. Said gas including oxygen the amount of at least equal to the alkali solution in the containing sulfur compound of salts of oxidized into *** sulphide need chemical calculating amount it is usually need chemical calculation amount is 2-4 times of. Said oxidizing agent is also can select or cooperate with the chosen oxidizing inorganic or organic oxygenated compound such as hydrogen peroxide and. And after oxidation treatment alkali solution sulphur in the compound of salt is transferred into *** sulfide alkali solution thus obtaining regeneration.

[0058] in step the obtained in step the content of the sulphur compound of salts of alkali liquid and oxidizing agent and oxidation catalyst and obtained in step a part of the de-sulfurization on the back of the heavy fraction when it is contacted with the tail gas discharging model can effectively avoid the alkali solution inclusion of air bubbles so as to influence the next recycle the alkali solution after desulphurization the desulphurization effect and light fraction effect of desulfuration.

[0059] according to this invention claims a method for using and it is convenient for system the continuous cycle operation of the said step is used for extracting alkali liquid in the *** of sulphide after desulphurization heavy distillate is obtained in step a part of the de-sulfurization on the back of the heavy distillate of the dosage of alkali liquor can be adjusted according to the actual amount and the generated in *** of sulfide content and the only can make the alkali liquid in the *** sulphide being extracted into the desulphurization and heavy fraction in which can preferably under the condition of said step is used for extracting alkali liquid in the *** sulphide a part of the obtained in step the desulphurization and heavy fraction of the complete desulphurization and heavy fraction of the weight ratio is i: 10-500 preferably i: 50-200.

[0060] according to this invention can be obtained in step the content of the sulphur compound of salts of alkali liquid and oxidizing agent and oxidation catalyst and obtained in step a part of the de-sulfurization back the heavy fraction of the contact mode can be known by various ways such as current contactor and mixed with counter current contact and so on mixing for example wherein said contact mode can be used without medium and the static mixer way or in hole board particle filler such as ceramic ring and so on ball nickel metal fibre or non-metal fibre or filament bundle shaped as medium the contact mode and load oxidation catalyst as medium contacting way of the load type oxide the catalyst can be described as above the metal phthalocyanine compound is the load type oxidation catalyst in the form of using the load type oxidation catalyst.

[0061] in this invention in step a step of obtaining the content of sulphur compound of salts of alkali liquid with a portion of the obtained in step of the desulfurizing and back of the heavy distillate of the proportion is not particularly limited the portion of the obtained in step of after desulphurization and heavy fraction of the amount can be adjusted according to containing sulphur compound of salts of alkali liquid in the sulphide are oxidized into sulphate *** oxide after alkali liquid in the *** of sulphide quantity is only can ensure that it can fully the alkali liquid generated in *** sulfide extract the heavy fraction can be preferably in the condition of the following steps obtaining the content of sulphur compound of salts of alkali and the obtained in step a part of the de-sulfurization on the back of the heavy distillate of the volume ratio is 1-500: 1 more preferably 5-200: *** are connected to the step is preferably 10-50: I.

[0062] according to the invention in step in said phase separation method can be used for the field of normal method for using it can ensure that it can obtain *** absorbs the sulphur compound of heavy distillate and after desulphurization by alkali liquid can be such as gravity sedimentation and separation.

[0063] in step in the alkali liquid in the *** sulphide being extracted into said then the heavy fraction of the in and carries out phase is separated from the liquid flowing body is divided into upper and lower two layers of the upper layer is set with *** sulphide the heavy fraction of the oil phase and the lower layer is then the alkali liquid phase. The extracting phase and in the process of separating *** sulphide from alkali liquid separated out of the extraction of the upper layer of the desulfurizing and back of the heavy distillate and the phase separation to obtain basically does not contain oxygen after desulphurization of the alkali liquid and absorbed the *** sulphide the heavy fraction.

[0064] the phase is separated from the phase separation system such as depositing and separating system to normal using such as steel wire and glass of coke and so on filling material as coalescent agent to promote *** sulfide poly to the heavy fraction of said contact so as to realize extracting and separating the staying time it can ensure of fully extracted it can be optimized 0 5-2 can be small *** inches to promote the step of separating the fully processed with. It is carried through phase disengagement in the sedimentation and separation it also can make the alkali solution in portable * of the residual gas including oxygen to obtain the step of releasing ***.

[0065] according to this invention claims a method for using the obtained in step of absorbing the *** sulphide the heavy fraction can be used circularly it ensures that after desulphurization of gasoline yield the method also comprises the step to obtain at least a part of said absorption the *** sulphide the heavy fraction of the returned to step to carry out the selective hydrogenation desulphurization or repeatedly used in step from step

To obtain a part of the de-sulfurization back the heavy fraction of the mixed repeatedly carry out alkaline solution regeneration and lye after desulphurization and again used for extracting alkali liquid in the *** sulphide and then returning to step in.

[0066] said step so as to obtain at least a portion of the absorbs *** of sulphide into heavy distillate of the content is not specifically defined according to actual condition such as is determined according to the second liquid alkali sulphide or the quantity of the obtained in step of absorbing the *** of sulfide in the heavy fraction *** of sulfide content according to the again extracted the extracted ability to the.

[0067] according to the invention preferably under the condition of the invention is to be favourable to heavy distillate a selective hydrogenation desulfurization process the method comprises the step

After between the step of the method further comprises the step of obtained in step of absorbing the *** sulphide the heavy fraction of the execute focusing structure process for removing wherein the content of micro alkali liquid and other mechanical impurity. The polymer structure method of processing can be used for the field of technical personnel known that the polymer structure method for processing such as the absorbent the *** sulphide the heavy fraction and coalescent agent usually used as steel wire and glass of coke and so on filling material as coalescent agent to promote the micro alkali liquid and other mechanical impurity adsorbing on the polymer adhesive and the contact of the stopping time can be 0 for 1-2 h inches.

[0068] according to the invention preferably under the condition of the method further comprises the step of obtained in step a part of the absorbs *** sulphide the heavy fraction with the following steps the tail gas are connected to absorption in tail gas of sulphur light hydrocarbon and the absorption *** sulphide the sourness of light hydrocarbon the heavy fraction of the returned to step to carry out the selective hydrogenation desulphurization. Can be obtained by tail gas by passing through the light hydrocarbon recycling device for recovering alkali solution with the air outlet of micro light hydrocarbon by using such as heavy hydrocarbon oil as the recycling method of recycling tank and so on.

[0069] preferably under the condition of the said absorption *** sulphide the sourness of light hydrocarbon the heavy fraction of the circularly used so it absorbs the sulphur compounds containing sulphur *** light hydrocarbon the heavy fraction of the returned to step to carry out the selective hydrogenation desulphurization.

[3] 0070 ] according to the invention uses the invention claims a method for the gas to do desulfurization obtained after the process of the desulfurizing and heavy fraction of the sulphur in the alcohol sulphur content is low the y 1-50 g per g between the optimized condition according to actual production demand in order to further and obtaining free sulphur and sulphur content is not more than ioy g/g of the product is of the product of ethanol gasoline sulfur sulphur content should not be larger than ioii g/g the method further comprises the step of obtained in step of said desulfurization on the back of the heavy distillate is obtained in step of said after desulphurization the light fraction of mixing to obtain the product before the obtained in step of said desulfurization on the back of the heavy distillate is obtained in step of said desulfurization on the back of the light fraction of the mixture carrying out deodorizing treatment; Or the obtained in step of the desulphurization and heavy fraction of the carrying out deodorizing treatment and then the obtained in step of said desulfurization on the back of the light fraction obtained from mixture of the product of the product obtained from the alcohol sulphur of sulphur content is not more than 10 g per g y. Wherein the aim of deodorization it adopts catalytic oxidation method of removing the heavy fraction hydrogenation process in order to not and carrying out hydrogenation of the invention claims a new generation of mercaptan *** the step of ensuring the refining of oil product thiol in sulfur content of not more than 10 i g/g.

[0071] according to the invention uses the invention claims a method for the gas to do desulfurization after processing it can obtain the total sulfur content is reduced gasoline product such as to obtain the gasoline product the sulfur content and it can meet the national iii discharging standard # specified car used in gasoline sulfur content of not more than 150 y g/g and iv # meets the national discharging standard of vehicle in gasoline sulfur content u is not more than 50 g/g the requirement of preferably under the condition of the gasoline product the sulfur content satisfies the predicted future v # national discharging standard of vehicle in gasoline sulfur content of not more than ioy g/g the requirement of.

[0072] according to this invention when the production target sulphur content is not more than ioy g/g of the gasoline product the request then the light fraction of total sulfur content of weight of at least is not more than ioy g/g and the requirement of desulphurization and heavy fraction of the total sulfur content of weight of at least and it is not more than iou g/g it can be flexibly adjusted light and heavy fraction of the cutting point temperature to make the light fraction after desulphurization sulphur includes a thiol sulphur weight weight of not more than 10 u g/g and the heavy distillate and selective hydrogenation treated containing sulfur comprising a thioalcohol sulphur weight weight of it is not more than ioy g/g after desulphurization the light fraction and after desulphurization and heavy distillate the method comprises the step after mixing and obtaining free sulphur and sulphur and sulphur content is not more than ioy g/g of the product according to the existing gasoline product thioalcohol sulphur index is not more than ioy G/g a prescribed by the selective hydrogenation treatment after the heavy distillate and the desulfurization alcohol and the light fraction after mixing it is not used by catalytic oxidation and deodorizing refinement to directly change to be sulphur content is not more than ioii G/g of low sulphur gasoline product

[0073] the obtained in step of said desulfurization on the back of the heavy distillate is obtained in step of said desulfurization on the back of the light fraction obtained from mixture of product is the sulphur content of weight are added is not more than ioil g/g is directly obtained from mixture of satisfy the expected v # national discharging standard sulphur content of the prescribed vehicle gasoline product. If the two sulphur content of weight is more than ioil g/g such as producing satisfy the need of national iii or iv # national discharging standard gasoline product the two mercaptan sulphur content of weight are added is not more than g ioiig or when it is not used and deodorizing processing and directly mixing to obtain the product not needing through the ozone processing and ensure product sulphate mercaptan content of not more than

10 g per g ii.

[0074] if adopting liquid catalytic oxidation method of oxidation catalyst is dissolved in lye or the alkali liquid to form a stable emulsion of metal phthalocyanine compound and said metal phthalocyanine compound in the alkali liquid in the content can be is 5-1000 ii g/g preferably 10-5001 ! g/g. As oxidizing agent the gas containing oxygen the oxygenated gas such as the front of said inner container defined is preferably an air purifying air the amount of at least equal to the hydrogenated heavy fraction from not and carrying out hydrogenation of the invention claims a new generation of mercaptan oxidized into *** sulphide need chemical calculating quantity is optimized to thioalcohol oxidized into *** sulphide need chemical calculation amount is 2-4 times of; Said oxidizing agent is also can select or cooperate with the chosen oxidizing inorganic or organic oxygenated compound such as hydrogen peroxide and.

[0075] if adopting the fixed bed catalytic oxidation method of the fixed bed catalyst for deodorized is supported on the porous material on metal phthalocyanine compounds are preferably under the condition that adopts a fixed-bed catalytic oxidation to carry out. Said fixing bed and deodorization system of the oxidant oxidizing agent is preferably an oxygen containing gas and preferably in alkali agent in the presence of obtained in step of after desulphurization and heavy fraction obtained in step the light fraction or mixture of the obtained in step of after desulphurization and heavy distillate of catalytic amount of the porous material as carrier of metal phthalocyanine compound contact carrying out deodorizing reaction.

[0076] wherein said fixing bed and deodorization system of the pressure can be 0 to 2 mpa l is optimized 0 2-0 8mpa. Fixed bed and deodorizing the temperature of the system can be below zero to 100 degree to 10 c c preferably 0-80° c after selective hydrogenation treatment after the liquid when the speed can be used as 0 i ioh ' is optimized 0 5-5 3' h

[0077] said fixing bed and deodorizing catalyst the carrier can be all kinds of the field of normal oxidation catalyst of the porous material the active component is metal phthalocyanine compound; The catalyst the total weight as the standard of the carrier content can be 90-99 9 weight% is preferably 95-99 9 weight%; Said metal phthalocyanine compound content can be 0 1-10 weight % and preferably is 0 1-5 wt %.

[0078] said alkali agent can be selected from the field of common any normal use of alkaline reagent such as inorganic alkali solution and / or alkaline organic compound water solution of the ideal inorganic alkali solution is generally of alkali metal and/or alkaline earth metal hydroxide water solution of and / or ammonia water such as said alkali metals and alkaline earth metal hydroxide can be selected from sodium hydroxide potassium hydroxide lithium hydroxide calcium hydroxide and barium hydroxide in *** or several kinds. Said alkaline organic compound water solution of alkaline organic compound can be organic amines compound biologic alkali compound and organic quaternary ammonium salt in *** one or several is preferably an organic quaternary ammonium salt. Said alkaline organic compound in the water solution of alkaline organic compound of which is 0 1 to 1000 u g/g preferably is 0 5-100 u g/g.

[0079] according to this invention when performing the deodorized inches no matter liquid catalytic oxidative mode is also fixed bed catalytic oxidative mode selected in the catalytic auxiliary agent the activator is carried out in the presence of the catalytic auxiliary agent can be polar compound and/or jae weng compound said polar compound can be selected from water methanol *** alcohol isopropyl alcohol and so on low carbon alcohol alkyl amine basic nitrogen compound and alkyl of amine compound basic nitrogen in the one or several ***. Jae weng said compound can be quaternary ammonium compound * wei wei weng compound wei shen wei weng compound paving wei weng compound oxygen weng wei compound and wei weng sulfonium compound of *** one or several as cation atom and n is 0 and method as p s and so on is preferably a quaternary ammonium salt and / or quaternary ammonium salt. And waiting for processing oil such as following steps of the heavy distillate of the light fraction or mixture of the heavy fraction is based on the weight of the catalytic auxiliary agent the amount can be 0 i ioooii g/g preferably is 0 5-500 ii g/g.

[0080] said alkaline reagent and the catalytic auxiliary agent can be connected with the waiting for processing oil after mixing it can be dipped in advance gastric or adsorbed on the catalyst carrier is set on the metal phthalocyanine which is used together. When the alkaline reagent in advance or soaking and absorbing the catalyst carrier is the effective weight alkali agent in the solvent the quality of the can cover total weight of catalyst of 0 1-40 weight percent preferably is 0 1-20 wt %.

[0081] in this invention of said metal phthalocyanine compound comprises the following steps the oxidation step and step of the deodorization is also in the step of using the metal phthalocyanine compound in the metal phthalocyanine can be chosen from magnesium titanium phthalocyanine phthalocyanine hafnium phthalocyanine copper phthalocyanine tantalum phthalocyanine key phthalocyanine manganese phthalocyaine iron phthalocyanine cobalt phthalocyanine molybdenum phthalocyanine copper phthalocyanine phthalocyanine palladium silver phthalocyanine zinc phthalocyanine and tin in the invention claims a phthalocyanine *** or more preferably cobalt phthalocyanine and /or vanadium phthalocyanine. Said metal phthalocyanine compound can be selected from the group consisting of metal phthalocyanine of sulfonic acid salts of carboxylic acid salt quaternary ammonium salt and its wei weng compound such as.

[0082] deodorization system and the use of metal phthalocyanine is preferably a positive and negative ions to metal phthalocyanine is provided with a positive ion radical metal phthalocyanine with negative ion radical metal phthalocyanine formed by the. Said with positive ion radical in metal phthalocyanine is selected from the group consisting of metal phthalocyanine of sulfonic acid salts of carboxylic acid salt preferably phthalocyanine cobalt sulfonic acid salt comprises at least one of cobalt phthalocyanine of formula a sulfonic acid salts and sulfonated phthalocyanine cobalt phthalocyanine cobalt sulfonic acid salts of the double double sulfonated phthalocyanine cobalt phthalocyanine cobalt sulfonic acid salts of the three third sulfonated phthalocyanine cobalt phthalocyanine cobalt sulfonic acid salts of 4 4 sulfonated phthalocyanine cobalt in the middle of one or any mixture. Said with negative ion radical in metal phthalocyanine is selected from the group consisting of metal phthalocyanine of quaternary ammonium salt compound wei weng preferably cobalt phthalocyanine quaternary ammonium salt of the general formula is as follow copc [ n r 1r2 r3 -a] a the pc which is used for the expression of phthalocyanine group the structure of the symbols *** r2 r3 is same or different with 1-3 carbon atoms a represents alkyl halide anion most preferably is a 1 is quaternary ammonium compound of the value is the - 1-4.

[0083] is said as following steps *** the oxidation step and step of deodorization in the step of using the fixed bed catalyst of the carrier can be selected from aluminium silicon containing alkaline earth metal transition metal rare earth metal and porous carbonaceous material such as aluminium oxide silicon oxide silicon aluminium hydrochloric acid calcium oxide magnesium oxide titanium oxide natural and artificial clay and artificial natural zeolite from mineral materials such as coal and petroleum and other plant material such as wooden meal the shell the core and so on and synthetic resin and so on the carbonaceous material and is preferably activated carbon. Porous carrier the specific surface it is usually used as 10-1500 g / m2 is preferably a / m2 100-1200 g.

[0084] according to the invention a preferred embodiment such as image i show:

[0085] said image i only represents a preference of the flow chart is not related to the container the heater the cooling pump compressor mixer valve *** process control equipment and so on the surface of details it only needs to know the technical field of people to know the invention is to said basic or not is showed easily the device case *.

[0086] gasoline raw material through the pipe line i enter into fractionating system 2 light fraction gasoline through pipe line 4 gasoline flowing out from the heavy distillate flows out from the line 3 and enters into the selective hydrogenation desulphurization system 28 through the first hydrogenation reaction zone the low activated hydrogen under the action of catalyst carrying out the first selective hydrogenation reaction and through the second hydrogenation reaction zone high activity hydrogenation under the action of catalyst to carry out the second selective hydrogenation reaction.

[0087] from the distillation system of light fraction gasoline 4 through pipe line the pumping system 5. Fresh alkali solution or a metal phthalocyanine of the catalyst alkali liquid from depositing and separating system 15 and the alkali solution then it is composed of pipe line 18 the outlet through pipe line 8 entering the pumping system 5 light fraction with the lye in the pumping system 5 is counter current contacting light fraction of the sulphide in mercaptan being extracted into the alkali solution to generate sulphide of salt mercaptide then the light fraction by pipe thread 7 away from the extraction system 5.

[0088] absorbs the sulphur compound of alkaline solution by pipe thread 7 flow into the oxidation and the pumping system 11 and through pipe line 9 enters in oxidation and the pumping system 11 a part of the desulphurization and heavy fraction 10 through pipe line is injected into the oxidizing agent is preferably with an oxygen-containing gas the mixed oxide and the pumping system 11 alkali solution in sulphuret the salt is oxygenated as *** sulphide the alkali liquid to get the regenerating at the same time *** sulphide is reflected in the extracting part after desulphurization and heavy fraction in. Normal if it is necessary to inches fresh alkali liquor and catalyst can be input through pipe line 8*10.

[0089] from oxidation and the pumping system 11 of the desulfurizing after lye absorbing *** the sulphur compound of heavy distillate and residual of the oxidant oxygen content of the gas mixture through pipe line 12 flow into the phase separation system the sedimentation and separation system 13 and 14 through the pipeline flowing into sedimentation and separation system 15 and the nitrogen and/ or basically without sulfur the gas through pipe line 16 is contacted with the step of replacing *** alkali solution in the memory of the air and it can move up and down through pipe line outlet 17. Essentially no oxygen of regenerating alkaline solution through pipe line 18 and the pipe line 8 is returned to the pumping system 5 is continuous using.

[0090] from depositing and separating system 13 the top part of flowing out of absorbed the *** sulphide the heavy fraction and redundant air through pipe line 19 into the depositing and separating system of 20 continuously depositing and separating. Redundant air through pipe line 22 discharging and flow into sulphur burning burning furnace and then releasing.

[0091] absorbs *** sulphide the heavy fraction of the through pipe line 21 inlet conglomerate removing system 24 through pipe line 23 a part of containing *** of sulphide hydrogenated heavy distillate and the pipe-line 9 return to oxidation and the pumping system 11 circularly used for *** sulfide reaction of extracting and removing less amount of alkali solution through pipe line 26 after it is discharged through pipe line 25 and the pipe line 3 and from the distillation system 2 the heavy fraction of the mixed flows into the selective hydrogenation system 28 carrying out selective hydrogenation desulfurization reaction hydrogen is composed of pipe flow into the wire 27.

[0092] the heavy distillate and hydrogen the low activated hydrogen catalyst with high activity of hydrogenation catalyst and under the action of the contact carrying out selective hydrogenation desulfurization reaction through the air to remove the sulfureted hydrogen and then it flows out after selective hydrogenation system 28.

[0093] hydrogenation product and through the air to remove the sulfureted hydrogen is divided into two parts of fluid wherein a small part of the hydrogenated heavy fraction of the fluid through pipe line is 30 to the pipe-line 9 flow into the oxidation and the pumping system 11 and extracting and alkali solution oxidation regeneration generated when *** sulphide but most of the hydrogenated heavy fraction of the fluid through pipe line 29 from pumping system 5 of the desulfurizing the light fraction through pipe line 6 then mixing and from the line 31 of the desulfurizing alcohol the activator through pipe line 32 flowing an oxidizing agent is preferably a mixed gas including oxygen flows into the fixed bed and deodorization system 33 of the heavy fraction in the presence of hydrogen in the process of newly generated the mercaptan to carry out oxidation * the product through pipe line 34 or after the sedimentation and then it flows out after.

[0094] is more than one combining the attached drawing detail description of the invention the preferred embodiment of this invention and it is not limited to the embodiment of the specific detail of the invention claims a technique concept range according to the technical scheme of the invention carrying out several is simple change of these variable model is simple and it belongs to the invention claims a protection range.

[0095] the need the invention is that the specific implementing manner in the description of each idiographic technology characteristic is not the contradiction of under the condition that can pass through any suitable to carry out combination in order to avoid unnecessary repeated this invention has various possible the combination way of the invention does not.

[0096] the invention all kinds of different embodiments are also can be any combination it only needs to back it is not illegal the invention the idea of the same should as the invention claims a content.

[0097] a lower surface by the specific embodiment of this invention to the first * the detailed description.

[0098] the embodiment of the two kinds of selective hydrogenation desulphurization catalyst is composed of china petroleum chemical industry stock co ltd catalyst ltd changling catalyst factory providing commodity number are respectively rsds ol low activity hydrogenation catalyst and rsds 02 high activity hydrogenation catalyst.

[0099] the embodiment of the content of sulphur * a method for the field of technical personnel the known method of the micro cullen.

[0100] embodiment i

- 0101 ] the embodiment is used for the invention the invention claims a desulphurizing method for gasoline.

[0102] in the embodiment of the attached drawing i show the flow i the surface of the raw material in catalytic cracking oil a processing.

[0103] gasoline a cutting part of the distillation temperature is 75° boiling range c obtaining relatively high heavy distillate boiling range and is relatively low the light fraction after cutting light fraction b and heavy fraction c of the yield is about 40 wt% radically 60 weight%.

V- 0104 ] [ the selective hydrogenation of the system of the heavy fraction carrying out selective hydrogenation processing the first selective hydrogenation reaction condition comprises: Reaction hydrogen partial pressure is i 6mpa reaction temperature 240° c the liquid air speed oh hydrogen oil 1 3 volume ratio 300 nm3 or m3. The second selective hydrogenation reaction condition comprises: Reaction hydrogen partial pressure is i 6mpa reaction temperature 290° c the liquid air speed oh 3 3' hydrogen oil volume than 300 nm3 or m3. The hydrogenated heavy fraction is divided into two parts a small part of the desulphurization and heavy distillate d and a large part after desulphurization heavy fraction e of weight ratio is i: 75.

[0105] the pumping system in alkali and the light fraction b and the volume ratio is 0 5: 1 the temperature is 20 0 c pressure *** 5mpa.

[0106] in the oxidation and the pumping system of alkali solution of sulfonated phthalocyanine cobalt from purchasing guangzhou large fine chemical industry factory of content is iooii g/g as oxidizing agent in oxygen gas injection amount of the alkali solution volume ratio is i: 4 5 oxide and the pumping system pressure *** is 0 34mpa temperature is 50 degrees c. Wherein said alkali liquid is quality percent concentration of 15%- of sodium hydroxide aqueous solution; The oxygen containing gas as the air and oxygen volume content of 21%. It is used for absorbing alkali solution in the sulfur compound of salts of *** oxidization to generate sulphide of a small part of the desulphurization and heavy distillate d and regenerating alkaline solution by volume ratio is i: 25.

[0107] the phase separation system in the sedimentation and separation system and the conglomeration separating system of filling medium is polypropylene fibre material the temperature of are all natural temperature 25° c pressure *** are natural pressure *** 0 impa phase separation is obtained after absorbing the *** sulphide a small part of hydrogenated heavy * and d and lye after desulphurization; And the absorption of *** sulphide a small part of hydrogenated heavy * of heavy distillate d and c mixing after selective hydrogenation system to perform hydro-treating.

[0108] most of the desulphurization and heavy fraction e from pumping system the light fraction b are mixed and then flows into the fixed bed deodorization system for mercaptan removal treatment. Wherein said fixing bed mercaptan removal system used as catalyst loaded on active carbon is set on the i by weight of sulfonated phthalocyanine cobalt from purchasing guangzhou large fine chemical industry factory of the reaction temperature is 40 degree centigrade c is 0 3mpa *** pressure the liquid air speed is 2 or oh

[0109] raw material a basic properties such as i surface of the raw material a after the processed result are respectively as surface i and the table 2.

[0110] the ratio i

[0111] to the proportion the invention claims a method for specification of the existing technology of gasoline desulfurization method.

[0112] adopts the embodiment of the same i raw material oil and a according to embodiment of the same i the combination of desulfurizing *** process of the same *** * a method for gasoline desulfurization different from the embodiment of the i used in back extraction after the regeneration of the alkali solution disulfide a small part of the desulphurization and heavy distillate d using the step of the raw material gasoline cutting part of the distillation to obtain the heavy fraction of the replacing the bidentata bo in step a selective hydrogenation desulphurization system only by using single rsds ol catalyst. And the back extraction after the regeneration of the alkali liquid in the *** of sulphide is composed of the step of the raw material gasoline cutting part of the distillation to obtain the heavy fraction of the user the embodiment of i used in a small part of the desulphurization and heavy distillate d using quantity of the same and the back extraction after the regeneration of the alkali solution disulfide then the structure processing and from the distillation system the remainder of the most of the heavy fraction of the mixing flow in the hydrogen system to be added hydrogen desulfurization process. Raw material a after the processed result are respectively as surface i and the table 2.

[0113] gage i

0114 ] [

<img id="idf0001" file="CN102851069AD00161.tif" img-content="drawing" img-format="tif" />

[0115] from the i the result can be seen through the invention claims a method for processing the raw material a of the desulfurizing rate reaches 95 percent the product of sulphur content is 40 u g/g meets the national # iv gasoline discharge standard the product of sulphur content u is not more than 50 g/g the requirement of the olefin saturation 22 is only the loss of 6% be ron only i 6 single position to the ratio i of the desulfurizing rate 94 of the product is only 4% of sulfur content of 52 u g/g olefin saturation ratio is 30 to achieve the aim of losing 0%- be ron each unit 2 7. It can be known and the ratio i comparing with the embodiment of this invention is i the invention claims a method of it has good desulfurization effect and more low octane number loss.

[0116] table 2

0117 ] [

<img id="idf0002" file="CN102851069AD00171.tif" img-content="drawing" img-format="tif" />

88

[0118] table 2 the invention claims desulfurizing regenerated after alkali solution in mercaptan content of sodium measuring data and uses 90-120° c petroleum ether and the sulphur free alkali solution after desulphurization embodiment i after desulphurization finger of the alkali solution is from the i flows from the pipeline 18 that the hydrogenated heavy fraction of the extraction *** of sulphide after desulphurization and so on the volume of alkali solution and mixing after separating the measured lye after desulphurization sulphur content in lye after desulphurization sulphur content in equal to the measured by petroleum ether sulphur content in. After desulphurization alkali solution in a mercaptan content of sodium in inches or more recycling the light fraction of extracting and desulfurizing is not good the alkali solution after desulphurization sulphur content in bigger one aspect the invention after desulphurization alkali solution in the memory of mercaptan content of sodium can be more *** the other side the invention after desulphurization alkali solution the portable * the heavy fraction can be any more than the phase separation system in alkali and the heavy distillate of the separation effect is bad.

[0119] is composed of the upper surface of i and the upper surface 2 in the data can be seen small part of the desulphurization and heavy distillate d can be used after the regeneration of the alkali liquid in the *** sulphide completely extract compared with the ratio i adopts the way of the small part not being desulphurization and heavy fraction of the effect is good.

0120 ] [ And the ratio i adopts the raw material after the steam of oil fractionation to obtain the heavy fraction of the extracting and removing the regeneration of the alkali liquid in the *** sulphide is obtained after desulphurization by alkali liquid in the residual sulfur content compared with the embodiment of this invention adopts i then the heavy fraction of the extracting and removing the regeneration of the alkali liquid in the *** sulphide is obtained after desulphurization by alkali liquid remain of sulphur content is smaller and the base in the alkali solution sulphur in the sodium alkoxide to and from the invention after desulphurization and heavy distillate and after desulphurization by alkali liquid in the phase separation system to separate the comparison is totally opposite to the ratio i after desulphurization of the alkali solution cooling the mixed into a small quantity of heavy distillate it is after desulphurization by alkali liquid in the memory of sulfur content of zeng and the heavy distillate and after desulphurization by alkali liquid in the phase separation system the separation effect of the relative weak so as to clamp with micro alkali solution of this part of heavy distillate it is possible to the follow-up of the hydrogenation system caused by bad influence

[0121] embodiment 2

[0122] this embodiment is used for the invention the invention claims a desulphurizing method for gasoline.

[0123] in the embodiment of the attached drawing i show the flow meter 3 the raw material in catalytic cracking gasoline f processing.

[0124] gasoline cutting and f of the distillation temperature is 60 degrees c so as to obtain relatively high boiling range of heavy distillate boiling range and is relatively low the light fraction after cutting light fraction and heavy fraction g h yield of respectively are 36 wt% weight percent 64.

[0125] the selective hydrogenation system in the first selective hydrogenation reaction reaction temperature is 290° c the second selective hydrogenation reaction reaction temperature is 310° oil c-reacting hydrogen volume ratio is 350 nm3 m3 and other conditions the embodiment of the following steps i with the same. The hydrogenated heavy fraction is divided into two parts small part of the hydrogenated heavy fraction m and most of the hydrogenated heavy fraction n weight ratio is about i: 150.

[0126] the pumping system in alkali and the light fraction g volume ratio is 0 2: 1 temperature to end face is c pressure *** impa.

[0127] in the oxidation and the pumping system of alkali solution of sulfonated phthalocyanine cobalt from purchasing guangzhou large fine chemical industry factory of content is 80y g/g with an oxygen-containing gas injection amount of the alkali solution volume ratio is i: 4 5 oxide and the extraction of the system 6mpa pressure *** temperature is 0 c 70°. Wherein said alkali liquid is quality percent concentration of 15%- of sodium hydroxide aqueous solution; The oxygen containing gas as the air and oxygen volume content of 21%. It is used for absorbing the regeneration of the alkali liquid in the *** of sulphide a little part after desulphurization and heavy * m and alkali regenerating solution by volume ratio is i: 10.

[0128] the phase separation system in the sedimentation and separation system and the conglomeration separating system of filling medium is polypropylene fibre material the temperature of are all natural temperature 25° c pressure *** are natural pressure *** 0 impa phase separation is obtained after absorbing the *** sulphide a small part of hydrogenated heavy * of m and lye after desulphurization; And the absorption of *** sulphide a small part of hydrogenated heavy * and heavy fraction h m and mixed and put into selectively adding hydrogen system to perform hydro-treating.

[0129] the closed deodorization system for as desulphurization alcohol and the light fraction of the hydrogenated heavy fraction then mixing the sulfur content of not more than ioii g/g mercaptan content of sulfur it is not more than ioii g/g. Raw material f of the basic properties and raw material f through the processed result if the surface of the display.

[0130] meter 3

0131 ] [

<img id="idf0003" file="CN102851069AD00181.tif" img-content="drawing" img-format="tif" />

[0132] 3 from the surface of the result can be seen through the method of this invention after processing the raw material f of the desulfurizing rate reaches 98 1% or more sulphur content of product is only 7 5i ! g/g not to meet the national v # gasoline discharge standard the content of sulphur in products is not more than ioy g/g the regulation of the olefin saturation is only the loss of 3 9 be ron only 0 4 each unit so it can be known that the embodiment of this invention claims a method of 2 it has good desulfurization effect and more low octane number loss.