CN106929098B - A kind of method of poor quality gasoline hydrogenation modification - Google Patents

A kind of method of poor quality gasoline hydrogenation modification Download PDF

Info

Publication number
CN106929098B
CN106929098B CN201511027275.5A CN201511027275A CN106929098B CN 106929098 B CN106929098 B CN 106929098B CN 201511027275 A CN201511027275 A CN 201511027275A CN 106929098 B CN106929098 B CN 106929098B
Authority
CN
China
Prior art keywords
gasoline
hydrogen
catalyst
product
hydrogenation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201511027275.5A
Other languages
Chinese (zh)
Other versions
CN106929098A (en
Inventor
钟海军
吕忠武
兰玲
鞠雅娜
李阳
姜增琨
葛少辉
赵秦峰
张学军
李天舒
袁晓亮
刘坤红
康宏敏
侯远东
王书芹
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Natural Gas Co Ltd
Original Assignee
China Petroleum and Natural Gas Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Natural Gas Co Ltd filed Critical China Petroleum and Natural Gas Co Ltd
Priority to CN201511027275.5A priority Critical patent/CN106929098B/en
Publication of CN106929098A publication Critical patent/CN106929098A/en
Application granted granted Critical
Publication of CN106929098B publication Critical patent/CN106929098B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The present invention discloses a kind of method of gasoline hydrogenation modification inferior, including (1) catalytic gasoline is mixed into pre-hydrogenator with hydrogen;(2) step (1) product enter fractionating column cut into it is light, in, heavy gasoline components;(3) for the light petrol component being ejected from fractionation column as reformulated gasoline blend component, the middle gasoline component and hydrogen that are come out from side line return to fractionating column after being mixed into the reaction of the first hydrodesulphurisatioreactors reactors;(4) heavy gasoline components and hydrogen come out from fractionation column bottom are mixed into hydro-upgrading reactor reaction;(5) product of step (4) is reacted into the second hydrodesulphurisatioreactors reactors;(6) after the cooling of step (5) product, into product separator gas-liquid separation, top hydrogen recycles, and bottom liquid phases enter stabilizer removing sulfurous gas, and reformulated gasoline product is mixed to get with light petrol.The method of the present invention reduces the loss of octane number in gasoline hydrogenation modification while alkene and sulfur content is greatly reduced.

Description

A kind of method of poor quality gasoline hydrogenation modification
Technical field
The present invention relates to a kind of hydrogenation modification method of catalytically cracked gasoline inferior, for reducing in catalytic gasoline sulphur and Olefin(e) centent reduces loss of octane number.
Background technology
China's haze weather occurs frequently in recent years, and the urban air-quality in the whole nation 70% is not up to standard, automobile exhaust pollution object row Put be big and medium-sized cities haze one of important sources, quality of gasoline upgrading, which becomes, reduces important arranging for automobile exhaust pollution object discharge It applies.70% or more component is catalytically cracked gasoline in China's motor petrol, has the characteristics that sulphur and olefin(e) centent are high, therefore vapour The key of oil quality upgrading is the sulphur and olefin(e) centent reduced in catalytic gasoline;But alkene is the main contributions of octane number Person will substantially lose the octane number of gasoline using conventional hydrodesulfurization Olefin decrease technology.How to realize catalytic gasoline both desulfurization, Olefin decrease, and the multiple target of octane number is kept, become China's quality of gasoline and upgrades significant technology issues in the urgent need to address.
Catalyzed gasoline hydrogenation desulfurization technology mainly divides two major classes both at home and abroad at present.One kind is selective hydrodesulfurization technology: By the improvement to technique and catalyst, inhibits the alkene saturated activity of catalyst, alkene quilt is avoided while hydrodesulfurization Excessive saturation, reduces the loss of octane number of hydrodesulfurization;Another kind of technology is catalytic gasoline modification technology:Hydrodesulfurization makes With conventional hydrogenation catalyst, then hydrodesulfurization gasoline is handled by the reaction such as isomerization, aromatisation, improves gasoline Octane number is to make up the loss of octane number in hydrodesulfurization.
ZL200410020932.9 discloses a kind of hydrogenation modification method of inferior patrol.This method is that a kind of full fraction is urged Change the process of gasoline hydrodesulfurizationmethod Olefin decrease.Under conditions of hydrogen exists and temperature gradually rises, with three kinds of catalyst Contact forms three reaction zones.First reaction zone temperature is relatively low, using Hydrobon catalyst, main pair removed in gasoline Alkene;Second, third reaction zone temperature is high, and second reaction zone uses gasoline reforming catalyst, carries out including aromatisation, isomerization Modification with benzene alkylation reaction is reacted, and the octane number of gasoline is improved, and improves product quality;Third reaction zone is added using selectivity Hydrogen desulphurization catalyst, organic sulfur compound during removing is oily to greatest extent.This method is fed using full fraction, and loss of octane number is larger.
ZL200410060574.4 discloses a kind of inferior patrol hydrogenation modifying process.Its technical process is:By raw material vapour Oil is cut into light fraction and heavy distillat at 60~90 DEG C, and wherein heavy distillat is first mixed with hydrogen, then is connect with Hydrobon catalyst Reaction is touched, the effluent after reaction is contacted with aromatization modification catalyst again carries out aromatization modification reaction, obtains high-octane rating Low-sulphur oil fraction;Heavy naphtha after modification is mixed with light fraction or through the pretreated light fraction of removal of mercaptans again, Up to product gasoline.This patent needs the method using alkali refining removal of mercaptans, can cause the discharge of the disagreeableness alkaline residue of environment.
ZL200910080111.7 discloses a kind of hydro-upgrading side of the ultra-deep desulfurization of inferior patrol-recovery octane number Method:Full distillation gasoline inferior is cut into light, heavy distillat, keeps light petrol and the de- diene catalyst of selectivity and desulfurization-hydro carbons more Branch hydroisomerization catalyst contacts;Heavy petrol is set to be contacted with catalyst for selectively hydrodesulfurizing in first segment reaction zone, then It is contacted with supplement desulfurization-hydro carbons list branched chain isomer/aromatization catalyst in second segment reaction zone;Treated by general gently, heavy distillat vapour Oil mixing, obtains clean gasoline product.This patent only carries out de- diene to the light petrol after inferior patrol fractionation and handles, and weight vapour Containing compared with homodiene hydrocarbon in oil distillate, the quick coking of catalyst for selectively hydrodesulfurizing can be caused, influence the cycle of operation.
ZL 201110035512.8 discloses a kind of method of inferior gasoline upgrading.This method is first to full distillation gasoline Carry out the de- diene processing of selectivity, then its be cut into it is light, in, weigh three components, light petrol reconciles directly as clean gasoline Component, middle gasoline component are introduced into hydro-upgrading reactor and carry out the reactions such as aromatisation, isomerization, be then mixed into heavy petrol Enter hydrodesulphurisatioreactors reactors.Sulphur, olefin(e) centent in gasoline can be greatly reduced in the method for the present invention, reduce upgrading processes In the loss of octane number that brings, but for handling the higher bad gasoline of thiophene content, octane number when V gasoline of producing country It loses larger;Because directly being cut to gasoline after pre-add hydrogen using the patented method, to ensure that light petrol sulfur content meets State V, which reconciles, to be required, and need to be controlled very low light petrol ratio (being less than 25m%), thiophene is switched in heavy petrol as possible, in causing Gasoline proportionality, olefin(e) centent rise;Due to hydro-upgrading unit Olefin decrease limited extent, heavy petrol and heavy petrol after modification After mixing, sulfur content, olefin(e) centent are higher, and when V gasoline of producing country need to carry out deep hydrodesulfurizationof, and octane number is caused to damage It loses big.
US 5413698 discloses a kind of process of two-stage method production low sulfur clean gasoline, first cuts FCC gasoline Fractionation is cut, heavy petrol first passes through hydrodesulfurization, then carries out hydro-upgrading again and restores octane number, obtained heavy petrol hydro-upgrading Product reconciles with light petrol product again.Although the technology can produce the clean gasoline for meeting IV sulphur index request of Europe, lead to simultaneously Loss of octane number caused by hydrodesulfurization, but the difficult clean gasoline for meeting production Europe V sulphur index requests can be restored by crossing hydro-upgrading.
Invention content
The main purpose of the present invention is to provide a kind of methods of gasoline hydrogenation modification inferior, to overcome the prior art Octane number reduces more, reformulated gasoline alkene and the higher defect of sulfur content during middle gasoline upgrading.
The object of the present invention is achieved like this, it is a kind of poor quality gasoline hydrogenation modification method, this method include with Lower step:
(1) enter pre-hydrogenator after catalytic gasoline is mixed with hydrogen, reacted in the presence of catalyst for pre-hydrogenation, Reaction condition is:1.0~3.0Mpa of hydrogen partial pressure, 100~260 DEG C of reaction temperature, 2.0~8.0h of volume space velocity-1, hydrogen oil volume Than 10~200v/v;
(2) step (1) product enters in fractionating column, in 0.5~1.0Mpa of tower top pressure, 90~130 DEG C of feeding temperature, tower Push up 70~110 DEG C of temperature, cut at 190~230 DEG C of column bottom temperature it is light, in, heavy gasoline components;
(3) the light petrol component being ejected from fractionation column is directly as reformulated gasoline blend component, from fractionating column side line Middle gasoline component and hydrogen out enters the first hydrodesulphurisatioreactors reactors after mixing, in the presence of mild hydrogenation desulphurization catalyst It is reacted, reaction condition is:1.0~3.0Mpa of hydrogen partial pressure, 200~300 DEG C of reaction temperature, 2.0~5.0h of volume space velocity-1, 200~400v/v of hydrogen to oil volume ratio, middle gasoline hydrodesulfurizationmethod product returns again in fractionating column;
(4) enter hydro-upgrading reactor after heavy gasoline components and the hydrogen mixing come out from fractionation column bottom, add hydrogen It is reacted in the presence of modifying catalyst, reaction condition is:1.0~3.0Mpa of hydrogen partial pressure, 320~450 DEG C of reaction temperature, volume 1.0~3.0h of air speed-1, 250~500v/v of hydrogen to oil volume ratio;
(5) product of step (4) enter the second hydrodesulphurisatioreactors reactors, in the presence of catalyst for selectively hydrodesulfurizing into Row reaction, reaction condition are:1.0~3.0Mpa of hydrogen partial pressure, 220~350 DEG C of reaction temperature, 2.0~5.0h of volume space velocity-1, hydrogen Oil volume is than 250~500v/v;
(6) after the cooling of step (5) product, gas-liquid separation is carried out into product separator, is come out at the top of product separator Hydrogen enters circulating hydrogen compressor after the processing of desulphurization of recycle hydrogen tower and recycles, and product separator bottom liquid phases product enters steady Tower is determined, in 0.7~1.2Mpa of tower top pressure, 140~200 DEG C of feeding temperature, 120~180 DEG C of tower top temperature, column bottom temperature 180 Sulfurous gas is removed under the conditions of~240 DEG C, reformulated gasoline product is mixed to get with light petrol.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein the catalyst for pre-hydrogenation carrier is preferred For the mixture of aluminium oxide, silica or both, active component is preferably one or more of the VIth B, the VIIIth race, by catalysis Agent weight 100% is counted, and active component oxide content is preferably 10~30%, and surplus is carrier.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein the catalyst for pre-hydrogenation specific surface area Preferably 100~300m2/ g, it is preferably 0.2~0.6ml/g that hole, which holds,.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein the mild hydrogenation desulphurization catalyst carries Body is preferably the mixture of aluminium oxide and hydrogen type molecular sieve, and active component is preferably one or more of the VIth B, the VIIIth race, The molecular sieve is preferably one or more of HZSM-5, HMCM-22, H β and HY, and the molecular sieve preferably accounts for catalyst weight The 10~60% of amount, active component oxide preferably accounts for the 5~15% of catalyst weight.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein the mild hydrogenation desulphurization catalyst ratio Surface area is preferably 200~400m2/ g, it is preferably 0.4~0.8ml/g that hole, which holds,.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein the catalyst for hydro-upgrading carrier is excellent It is selected as aluminium oxide and the compound of molecular sieve, active component is preferably one or more of the VIth B, the VIIIth race, the molecule Sieve is preferably one or more of ZSM-5, Beta, SAPO molecular sieve, and in terms of catalyst weight 100%, the molecular sieve contains Amount preferably 60~90%, the active component oxide content is preferably 1~10%.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein the catalyst for hydro-upgrading specific surface Product is preferably 200~500m2/ g, it is preferably 0.2~0.5ml/g that hole, which holds,.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein preferably, the selective hydrogenation is de- Sulfur catalyst is with Al2O3、SiO2、TiO2And ZrO2One or more of be carrier, with P2O5、K2One kind or several in O and MgO Kind is auxiliary agent, and active component is one or more of VI B races, VIII race, based on catalyst weight 100%, active component oxidation Object accounts for 6~20%, and auxiliary agent accounts for 1~15%, and surplus is carrier;The catalyst for selectively hydrodesulfurizing specific surface area be 170~ 270m20.3~0.6ml/g of/g, Kong Rongwei.
The method of poor quality gasoline hydrogenation modification of the present invention, wherein preferably, the catalytic gasoline is to urge Change cracking gasoline, sulfur content is less than or equal to 1000mg/kg, and olefin(e) centent is less than or equal to 45v%.
Beneficial effects of the present invention:
1, using the pre- hydrogenation technique of full distillation gasoline, the diene content in gasoline is reduced, and be greatly reduced in light petrol Mercaptans content avoid the discharge of the disagreeableness alkaline residue of environment instead of alkali refining removal of mercaptans process, alkadienes in heavy petrol Content is reduced, and substantially extends the cycle of operation of Hydrobon catalyst;
2, use be cut into after the pre- hydrogenation technique of full fraction it is light, in, three component of heavy petrol, middle gasoline component hydrodesulfurization The flow that fractionating column is cut again is returned again to afterwards, which can be greatly reduced middle gasoline component section sulfur content, therefore relative to complete The flow directly cut after fraction pre-add hydrogen can be improved light petrol cutting ratio, reduce heavy petrol alkene and sulfur content, subtract Loss of octane number caused by few heavy petrol hydrodesulfurization is specially adapted to the high bad gasoline of processing thiophene content;
3, using the flow of " the hydro-upgrading back end hydrogenation desulfurization of heavy petrol elder generation ", relative to " after the hydrodesulfurization of heavy petrol elder generation plus The olefin(e) centent of the flow of hydrogen modification ", heavy petrol hydro-upgrading unit feed is high, can ensure the high aromatization rate of gasoline, subtract Few loss of octane number;Since catalyst for hydro-upgrading is with hydrodesulfurization function, heavy petrol experienced first slight desulfurization, The relay sweetening process of deep desulfuration again is also beneficial to reduce loss of octane number.
Description of the drawings
Fig. 1 is the flow chart of institute's poor quality gasoline hydrogenation method for modifying of the invention.
Specific implementation mode
It elaborates below to the embodiment of the present invention:The present embodiment is carried out lower based on the technical solution of the present invention Implement, gives detailed embodiment and process, but protection scope of the present invention is not limited to following embodiments, following implementation Test method without specific conditions in example, usually according to normal condition.
The present invention gasoline hydrogenation inferior modification method be:Catalytic gasoline and hydrogen are mixed into pre-hydrotreating reaction Device removes alkadienes;Pre- hydrogenation products enter fractionating column by gasoline be cut into it is light, in, three components of heavy petrol;It is come out from tower top Light petrol component directly as clean gasoline blend component, from the middle gasoline component of fractionating column lateral line withdrawal function be introduced into first plus Hydrogen desulfurization reactor carries out mild hydrogenation desulphurization reaction, and product, which returns again to fractionating column, to be continued to cut;It is come out from fractionation column base Heavy gasoline components are introduced into hydro-upgrading reactor and carry out the reactions such as mild hydrogenation desulfurization and aromatisation, isomerization, and heavy petrol adds Hydrogen product enters back into the second hydrodesulphurisatioreactors reactors and carries out deep hydrodesulfurizationof reaction;It is come out from the second hydrodesulphurisatioreactors reactors After material cooling, gas-liquid separation is carried out into product separator;The hydrogen come out from gas-liquid separator recycles after desulfurization process It uses, liquid-phase product enters after stabilizer removing lighter hydrocarbons and hydrogen sulfide is mixed to get final reformulated gasoline product with light petrol.
The technological process of the present invention can also be expressed as:Enter pre-hydrogenator after gasoline stocks and hydrogen are mixed, In 1.0~3.0Mpa of hydrogen partial pressure, 100~260 DEG C of reaction temperature, 2.0~8.0h of volume space velocity-1, 10~200v/ of hydrogen to oil volume ratio It is contacted with catalyst for pre-hydrogenation under the conditions of v and carries out hydrogenation reaction, the diene selective of easy green coke in catalytic gasoline is saturated into list Alkene, and low boiling point mercaptan in light petrol is transferred in heavy petrol by diene thioetherification reaction.Pre- hydrogenation products enter back into Fractionating column, in 0.5~1.0Mpa of tower top pressure, 90~130 DEG C of feeding temperature, 70~110 DEG C of tower top temperature, column bottom temperature 190 Under the conditions of~230 DEG C by gasoline be divided into it is light, in, heavy constituent;Middle gasoline enters the first hydrodesulfurization reaction after being mixed with hydrogen Device, in 1.0~3.0Mpa of hydrogen partial pressure, 200~300 DEG C of reaction temperature, 2.0~5.0h of volume space velocity-1, hydrogen to oil volume ratio 200~ Mild hydrogenation desulphurization reaction is carried out with mild hydrogenation hydrodesulfurization catalyst under 400v/v, middle gasoline hydrogenation product returns again to fractionation Tower is fed;From fractionation column base come out heavy petrol mixed with hydrogen after be introduced into hydro-upgrading reactor, hydrogen partial pressure 1.0~ 3.0Mpa, 320~450 DEG C of reaction temperature, 1.0~3.0h of volume space velocity-1, under the conditions of 250~500v/v of hydrogen to oil volume ratio with plus Hydrogen modifying catalyst contacts, and hydrodesulfurization, aromatisation and isomerization reaction occurs, while with reactions such as a small amount of alkene saturations. Hydro-upgrading reaction product enters back into the second hydrodesulphurisatioreactors reactors, in 1.0~3.0Mpa of hydrogen partial pressure, reaction temperature 220~350 DEG C, 2.0~5.0h of volume space velocity-1, contacted with catalyst for selectively hydrodesulfurizing under the conditions of 250~500v/v of hydrogen to oil volume ratio into Row deep hydrodesulfurizationof reacts, and after the cooling of hydrodesulfurization product, is detached into product separator and carries out gas-liquid separation.From gas-liquid point From device come out hydrogen recycled after desulfurization process, liquid-phase product enters product stabilizer, tower top pressure 0.7~ Gasoline is removed under the conditions of 1.2Mpa, 140~200 DEG C of feeding temperature, 120~180 DEG C of tower top temperature, 180~240 DEG C of column bottom temperature The lighter hydrocarbons and hydrogen sulfide of middle dissolving, are finally mixed to get reformulated gasoline product with light petrol.
Wherein, under the above-mentioned reaction condition of the first hydrodesulphurisatioreactors reactors, in catalytic gasoline 30 in gasoline component~ 50% sulfur-containing compound will be hydrogenated removing, while the removal efficiency of thiophene is more than 60%, and alkene saturation factor is less than 10%;From fractionation The light petrol component that tower top comes out can be directly entered products pot as clean gasoline blend component, can also be through Etherification of Light FCC Gasoline Cell processing is re-used as clean gasoline blend component after promoting light petrol octane number;The heavy gasoline components come out from Fractionator Bottom Hydro-upgrading reactor is initially entered with hydrogen mixing, is contacted with catalyst for hydro-upgrading, carries out mild hydrogenation desulfurization and alkene Isomery aromatization, by heavy gasoline components sulfur content hydrogenation and removing 20~50%;The heavy vapour come out from hydro-upgrading reactor Oily hydrogenation products enter back into the second hydrodesulphurisatioreactors reactors, are contacted with catalyst for selectively hydrodesulfurizing, and sulfur content plus hydrogen are taken off Remove to less than 50mg/kg (IV gasoline standard of state) or be less than 10mg/kg (state V and the above gasoline standard).
The present invention is suitable for the hydro-upgrading of catalytically cracked gasoline inferior, and gasoline upgrading technique of the invention uses full fraction Gasoline pretreatment then by fractionating column by catalytic gasoline be separated into it is light, in, weigh three components, after middle gasoline mild hydrogenation desulfurization Fractionating column is returned to, heavy petrol is using first hydro-upgrading and then the technological process of hydrodesulfurization.
When the method for the present invention produces sulfur content less than IV gasoline blend component of 50mg/kg states, research octane number (RON) loss is small In 1.0 units;When producing sulfur content less than V gasoline blend component of 15mg/kg states, research octane number (RON) loss is less than 2.0 Unit;The yield of blend gasoline product is all higher than 99.0w%.
Each catalyst used in following comparative example, embodiment is identical, and specific preparation process is exemplified below:
(1) catalyst for pre-hydrogenation:Industrial alumina powder 100g is taken, 50g water is added, is mediated, extrusion molding, 120 DEG C of drying, 500 DEG C roast 4 hours, then are roasted 4 hours at 900 DEG C, obtain catalyst carrier.It is molten by being stirred in 14g ammonium molybdates addition 45g water Solution, adds 75g nickel nitrates, 12g citric acids, catalyst activity metal impregnation liquid is made in stirring and dissolving.By catalyst carrier plus Entering in above-mentioned maceration extract, taken out after being impregnated 3 hours under room temperature, is aged 12 hours, then 120 DEG C of drying, 500 DEG C roast 4 hours, Finished catalyst A (referring to ZL201210367401.1, being not limited to this method) is made.
(2) mild hydrogenation desulphurization catalyst:Industrial boehmite powder 84g, H beta-molecular sieve 40g is taken, sesbania powder 4g, nitre are added Sour 3.5g, water 105g are mediated, extrusion molding, and 120 DEG C of drying, 500 DEG C roast 4 hours, obtain catalyst carrier.By 10g molybdic acids Ammonium is added in 55g water and stirs, and 6g phosphoric acid, 5g cobalt nitrates, 5g nickel nitrates is added, and the leaching of catalyst activity metal is made in stirring and dissolving Stain liquid.Using above-mentioned metallic solution impregnated catalyst support, it is aged 6 hours, then 120 DEG C of drying, 500 DEG C roast 4 hours, system Obtain finished catalyst B (being not limited to this method).
(3) catalyst for hydro-upgrading:HZSM-5 molecular sieves 150g, alumina powder 40g are taken, a concentration of 3g/ of 150ml are added The dilute nitric acid solution of 100ml is mediated, extrusion molding, and 120 DEG C of drying, 500 DEG C roast 4 hours, obtain catalyst carrier.It takes It states carrier 100g to be put into the solution of 200ml molybdenums, nickel, lanthanum, solution concentration MoO3 10g/100ml、NiO 3.5g/100ml、 La2O31.6g/100ml impregnates 2 hours under room temperature, and by 120 DEG C of drying of catalyst after separation of solid and liquid, 500 DEG C roast 4 hours, system Obtain finished catalyst C (referring to ZL200410074059.1, being not limited to this method).
(4) catalyst for selectively hydrodesulfurizing:Take ZrO made from 50g2-Al2O310g kaliophilites, 1.25g is added in powder Sesbania powder, 30ml water are mediated, extrusion molding, and 120 DEG C of drying, 550 DEG C roast 4 hours, obtain catalyst carrier.Weigh 13g nitre Sour cobalt, 15g ammonium molybdates EDTA, weak aqua ammonia complexing dissolving, add 10g ammonium dihydrogen phosphates, 15g magnesium nitrates, stirring and dissolving, system At catalyst activity metal impregnation liquid.Using above-mentioned metallic solution impregnated catalyst support, it is aged 4 hours, then 120 DEG C of bakings Dry, 450 DEG C roast 4 hours, and finished catalyst D (referring to ZL201010252648.X, being not limited to this method) is made.
Comparative example 1
Using a kind of catalytically cracked gasoline as raw material, property is shown in Table the catalytic gasoline 1 listed by 1.Catalytic gasoline is first in hydrogen point Press 2.2Mpa, 110 DEG C of reaction temperature, volume space velocity 3.0h-1, hydrogen to oil volume ratio 10:Located in advance using A catalyst under the conditions of 1 Reason cuts into light, two components of heavy petrol subsequently into fractionating column, fractionation column pressure on top surface 0.7Mpa, 120 DEG C of feeding temperature, 80 DEG C of tower top temperature, 205 DEG C of column bottom temperature, heavy naphtha accounts for the 65% of raw material.Heavy petrol is mixed into hydrogen first to be added Hydrogen reforming reactor is in hydrogen partial pressure 2.0MPa, 370 DEG C of reaction temperature, volume space velocity 1.22h-1, hydrogen to oil volume ratio 250:1 reaction Under the conditions of using C catalyst carry out hydro-upgrading, subsequently into hydrodesulphurisatioreactors reactors in hydrogen partial pressure 1.8MPa, reaction temperature 255 DEG C, volume space velocity 2.44h-1, hydrogen to oil volume ratio 250:Hydrodesulfurization is carried out using D catalyst under the conditions of 1, after product cooling Gas-liquid separation is carried out into product separator, the hydrogen come out at the top of product separator enters after recycle hydrogen sulphur tower desulfurization process Circulating hydrogen compressor recycles, and product separator bottom liquid phases product enters stabilizer, in tower top pressure 0.85Mpa, charging 155 DEG C of temperature, 145 DEG C of tower top temperature remove sulfurous gas under the conditions of 215 DEG C of column bottom temperature, are mixed to get with light petrol component Clean gasoline product.Process conditions and generation oil nature are shown in Table 2.From table 2 it can be seen that product sulfur content is 41mg/kg, desulfurization Rate 89.3%, olefin(e) centent drop to 26.0% from 41.0%, and octane number (RON) loses 1.2 units.
Comparative example 2
The feedstock oil that comparative example 2 uses is identical as comparative example 1.Catalytic gasoline is first in hydrogen partial pressure 2.2Mpa, reaction temperature 120 DEG C, volume space velocity 3.0h-1, hydrogen to oil volume ratio 10:It is pre-processed using A catalyst under the conditions of 1, is cut subsequently into fractionating column At light, two components of heavy petrol, fractionation column pressure on top surface 0.7Mpa, 115 DEG C of feeding temperature, 70 DEG C of tower top temperature, column bottom temperature 200 DEG C, heavy naphtha accounts for the 80% of raw material.Heavy petrol is mixed into hydro-upgrading reactor in hydrogen partial pressure with hydrogen first 2.0MPa, 380 DEG C of reaction temperature, volume space velocity 1.5h-1, hydrogen to oil volume ratio 300:It is carried out using C catalyst under 1 reaction condition Hydro-upgrading, subsequently into hydrodesulphurisatioreactors reactors in hydrogen partial pressure 1.8MPa, 275 DEG C of reaction temperature, volume space velocity 3.0h-1, hydrogen Oil volume is than 300:Hydrodesulfurization is carried out using D catalyst under the conditions of 1, entering product separator after product cooling carries out gas-liquid point From the hydrogen at the top of product separator out enters circulating hydrogen compressor after recycle hydrogen sulphur tower desulfurization process and recycles, production Product separator bottom liquid-phase product enters stabilizer, in tower top pressure 0.88Mpa, 150 DEG C of feeding temperature, and 140 DEG C of tower top temperature, Sulfurous gas is removed under the conditions of 210 DEG C of column bottom temperature, clean gasoline product is mixed to get with light petrol component.Process conditions and life It is shown in Table 2 at oil nature.From table 2 it can be seen that product sulfur content is 11mg/kg, desulfurization degree 97.1%, olefin(e) centent is from 41v% Drop to 22.3v%, octane number (RON) loses 2.2 units.
Comparative example 3
The feedstock oil that comparative example 3 uses is identical as comparative example 1.Catalytic gasoline is first in hydrogen partial pressure 2.2Mpa, reaction temperature 120 DEG C, volume space velocity 3.0h-1, hydrogen to oil volume ratio 10:It is pre-processed using A catalyst under the conditions of 1, is cut subsequently into fractionating column At it is light, in, three components of heavy petrol, fractionation column pressure on top surface 0.7Mpa, 118 DEG C of feeding temperature, 75 DEG C of tower top temperature, bottom of tower temperature 202 DEG C of degree, middle gasoline fraction accounts for the 50% of raw material, and heavy naphtha accounts for the 20% of raw material.Middle gasoline is mixed into hydrogen first Enter the first hydrodesulphurisatioreactors reactors, in hydrogen partial pressure 2.2MPa, 230 DEG C of reaction temperature, volume space velocity 3.13h-1, hydrogen to oil volume ratio 300:Hydrodesulfurization is carried out using B catalyst under 1 reaction condition, product returns again to fractionating column charging;Heavy petrol is first and hydrogen Gas is mixed into hydrodesulphurisatioreactors reactors in hydrogen partial pressure 1.8MPa, 250 DEG C of reaction temperature, volume space velocity 3.0h-1, hydrogen to oil volume ratio 300:Hydrodesulfurization is carried out using D catalyst under the conditions of 1, subsequently into hydro-upgrading reactor in hydrogen partial pressure 2.0MPa, reaction 380 DEG C of temperature, volume space velocity 1.5h-1, hydrogen to oil volume ratio 300:Under 1 reaction condition hydro-upgrading, production are carried out using C catalyst Enter product separator after product cooling and carry out gas-liquid separation, the hydrogen at the top of product separator out through recycle hydrogen sulphur tower desulfurization at Enter circulating hydrogen compressor after reason to recycle, product separator bottom liquid phases product enters stabilizer, in tower top pressure 0.88Mpa, 153 DEG C of feeding temperature, 143 DEG C of tower top temperature remove sulfurous gas under the conditions of 212 DEG C of column bottom temperature, with light petrol Component is mixed to get clean gasoline product.Process conditions and generation oil nature are shown in Table 2.From table 2 it can be seen that product sulfur content is 10mg/kg, desulfurization degree 97.4%, olefin(e) centent drop to 24v% from 41v%, and octane number (RON) loses 1.8 units.
Embodiment 1
The feedstock oil that embodiment 1 uses is identical as comparative example 1.Catalytic gasoline is first in hydrogen partial pressure 2.2Mpa, reaction temperature 110 DEG C, volume space velocity 3.0h-1, hydrogen to oil volume ratio 10:It is pre-processed using A catalyst under the conditions of 1, is cut subsequently into fractionating column At it is light, in, three components of heavy petrol, fractionation column pressure on top surface 0.7Mpa, 122 DEG C of feeding temperature, 85 DEG C of tower top temperature, bottom of tower temperature 210 DEG C of degree, middle gasoline fraction accounts for the 40% of raw material, and heavy naphtha accounts for the 20% of raw material.Middle gasoline is mixed into hydrogen first Enter the first hydrodesulphurisatioreactors reactors, in hydrogen partial pressure 2.2MPa, 220 DEG C of reaction temperature, volume space velocity 2.5h-1, hydrogen to oil volume ratio 250:Hydrodesulfurization is carried out using B catalyst under 1 reaction condition, product returns again to fractionating column charging;Heavy petrol is first and hydrogen Gas is mixed into hydro-upgrading reactor in hydrogen partial pressure 2.0MPa, 370 DEG C of reaction temperature, volume space velocity 1.22h-1, hydrogen oil volume Than 250:Hydro-upgrading is carried out using C catalyst under 1 reaction condition, subsequently into hydrodesulphurisatioreactors reactors in hydrogen partial pressure 1.8MPa, 235 DEG C of reaction temperature, volume space velocity 2.44h-1, hydrogen to oil volume ratio 250:It is carried out plus hydrogen using D catalyst under the conditions of 1 Desulfurization enters product separator and carries out gas-liquid separation after product cooling, the hydrogen come out at the top of product separator is through recycle hydrogen sulphur Enter circulating hydrogen compressor after tower desulfurization process to recycle, product separator bottom liquid phases product enters stabilizer, in tower top Pressure 0.87Mpa, 158 DEG C of feeding temperature, 146 DEG C of tower top temperature remove sulfurous gas under the conditions of 218 DEG C of column bottom temperature, and light Gasoline component is mixed to get clean gasoline product.Process conditions and generation oil nature are shown in Table 2.From table 2 it can be seen that product sulphur contains It is 40mg/kg to measure, desulfurization degree 89.5%, and olefin(e) centent drops to 27.8v% from 41v%, and octane number (RON) loses 0.4 list Position.
Embodiment 2
The feedstock oil that embodiment 2 uses is identical as comparative example 2.Catalytic gasoline is first in hydrogen partial pressure 2.2Mpa, reaction temperature 120 DEG C, volume space velocity 3.0h-1, hydrogen to oil volume ratio 10:It is pre-processed using A catalyst under the conditions of 1, is cut subsequently into fractionating column At it is light, in, three components of heavy petrol, fractionation column pressure on top surface 0.7Mpa, 118 DEG C of feeding temperature, 75 DEG C of tower top temperature, bottom of tower temperature 202 DEG C of degree, middle gasoline fraction accounts for the 50% of raw material, and heavy naphtha accounts for the 20% of raw material.Middle gasoline is mixed into hydrogen first Enter the first hydrodesulphurisatioreactors reactors, in hydrogen partial pressure 2.2MPa, 230 DEG C of reaction temperature, volume space velocity 3.13h-1, hydrogen to oil volume ratio 300:Hydrodesulfurization is carried out using B catalyst under 1 reaction condition, product returns again to fractionating column charging;Heavy petrol is first and hydrogen Gas is mixed into hydro-upgrading reactor in hydrogen partial pressure 2.0MPa, 380 DEG C of reaction temperature, volume space velocity 1.5h-1, hydrogen to oil volume ratio 300:Hydro-upgrading is carried out using C catalyst under 1 reaction condition, subsequently into hydrodesulphurisatioreactors reactors in hydrogen partial pressure 1.8MPa, 255 DEG C of reaction temperature, volume space velocity 3.0h-1, hydrogen to oil volume ratio 300:It is carried out using D catalyst under the conditions of 1 plus hydrogen is de- Sulphur enters product separator and carries out gas-liquid separation after product cooling, the hydrogen come out at the top of product separator is through recycle hydrogen sulphur tower Enter circulating hydrogen compressor after desulfurization process to recycle, product separator bottom liquid phases product enters stabilizer, in tower top pressure Power 0.88Mpa, 153 DEG C of feeding temperature, 143 DEG C of tower top temperature remove sulfurous gas under the conditions of 212 DEG C of column bottom temperature, with light vapour Oil ingredient is mixed to get clean gasoline product.Process conditions and generation oil nature are shown in Table 2.From table 2 it can be seen that product sulfur content For 10mg/kg, desulfurization degree 97.4%, olefin(e) centent drops to 26.5v% from 41v%, and octane number (RON) loses 1.0 units.
Embodiment 3
The feedstock oil that embodiment 3 uses is shown in Table the catalytic gasoline 2 listed by 1.Catalytic gasoline is first in hydrogen partial pressure 2.2Mpa, reaction 120 DEG C of temperature, volume space velocity 3.0h-1, hydrogen to oil volume ratio 10:Pre-processed using A catalyst under the conditions of 1, subsequently into point Evaporate tower cut into it is light, in, three components of heavy petrol, fractionation column pressure on top surface 0.7Mpa, 116 DEG C of feeding temperature, tower top temperature 73 DEG C, 203 DEG C of column bottom temperature, middle gasoline fraction accounts for the 47% of raw material, and heavy naphtha accounts for the 21% of raw material.Middle gasoline is first and hydrogen Gas is mixed into the first hydrodesulphurisatioreactors reactors, in hydrogen partial pressure 2.2MPa, 240 DEG C of reaction temperature, volume space velocity 3.0h-1, hydrogen oil Volume ratio 300:Hydrodesulfurization is carried out using B catalyst under 1 reaction condition, product returns again to fractionating column charging;Heavy petrol is first First and hydrogen is mixed into hydro-upgrading reactor in hydrogen partial pressure 2.0MPa, 380 DEG C of reaction temperature, volume space velocity 1.5h-1, hydrogen oil Volume ratio 300:Hydro-upgrading is carried out using C catalyst under 1 reaction condition, subsequently into hydrodesulphurisatioreactors reactors in hydrogen partial pressure 1.8MPa, 265 DEG C of reaction temperature, volume space velocity 2.5h-1, hydrogen to oil volume ratio 300:It is carried out using D catalyst under the conditions of 1 plus hydrogen is de- Sulphur enters product separator and carries out gas-liquid separation after product cooling, the hydrogen come out at the top of product separator is through recycle hydrogen sulphur tower Enter circulating hydrogen compressor after desulfurization process to recycle, product separator bottom liquid phases product enters stabilizer, in tower top pressure Power 0.87Mpa, 151 DEG C of feeding temperature, 142 DEG C of tower top temperature remove sulfurous gas under the conditions of 210 DEG C of column bottom temperature, with light vapour Oil ingredient is mixed to get clean gasoline product.Process conditions and generation oil nature are shown in Table 2.From table 2 it can be seen that product sulfur content For 12mg/kg, desulfurization degree 98.0%, olefin(e) centent drops to 25v% from 40v%, and octane number (RON) loses 1.2 units.
Table 1
Table 2
Comparative result when comparative example 1 and embodiment 1 are IV gasoline products of producing country, comparative example 2 are production with embodiment 2 Comparative result when V gasoline products of state.The main distinction is that the embodiment of the present invention 1, embodiment 2 contain " middle gasoline pumping Go out, mild hydrogenation desulfurization " processing unit, and comparative example 1, comparative example 2 do not have.Processing sulphur is contained it can be seen from 2 result of table The catalytic gasoline of 382mg/kg, alkene 41.0v% are measured, under IV scheme of state, 89.5% desulfurization degree, embodiment 1 is pungent compared with comparative example 1 Alkane value loses 0.8 unit less;Under V scheme of state, 97.4% identical desulfurization degree, embodiment 2 is lost less compared with 2 octane number of comparative example 1.2 units;
Comparative result when comparative example 3 and embodiment 2 are V gasoline products of producing country.The main distinction is the reality of the present invention Flow of the example 2 using " the hydro-upgrading back end hydrogenation desulfurization of heavy petrol elder generation " is applied, and comparative example 3 is using " after the hydrodesulfurization of heavy petrol elder generation The flow of hydro-upgrading ".It can be seen from 2 result of table under V scheme of state, 97.4% identical desulfurization degree, embodiment 2 relatively compares 3 octane number of example loses 0.8 unit less;In addition, using the method for the present invention processing sulfur content 695mg/kg, alkene 40v% it is another A kind of catalytic gasoline, under 98.3% desulfurization degree, alkene reduces 15v%, and octane number only loses 1.2 units.
Beneficial effects of the present invention:
1, using the pre- hydrogenation technique of full distillation gasoline, the diene content in gasoline is reduced, and be greatly reduced in light petrol Mercaptans content avoid the discharge of the disagreeableness alkaline residue of environment instead of alkali refining removal of mercaptans process, alkadienes in heavy petrol Content is reduced, and substantially extends the cycle of operation of Hydrobon catalyst;
2, use be cut into after the pre- hydrogenation technique of full fraction it is light, in, three component of heavy petrol, middle gasoline component hydrodesulfurization The flow that fractionating column is cut again is returned again to afterwards, which can be greatly reduced middle gasoline component section sulfur content, therefore relative to complete The flow directly cut after fraction pre-add hydrogen can be improved light petrol cutting ratio, reduce heavy petrol alkene and sulfur content, subtract Loss of octane number caused by few heavy petrol hydrodesulfurization is specially adapted to the high bad gasoline of processing thiophene content;
3, using the flow of " the hydro-upgrading back end hydrogenation desulfurization of heavy petrol elder generation ", relative to " after the hydrodesulfurization of heavy petrol elder generation plus The olefin(e) centent of the flow of hydrogen modification ", the charging of heavy petrol reforming unit is high, can ensure the high aromatization rate of gasoline, reduces pungent Alkane value is lost;Since catalyst for hydro-upgrading is with hydrodesulfurization function, heavy petrol experienced first slight desulfurization, then deep The relay sweetening process for spending desulfurization is also beneficial to reduce loss of octane number.
Certainly, the present invention can also have other various embodiments, without deviating from the spirit and substance of the present invention, ripe Various corresponding change and deformations, but these corresponding change and deformations can be made according to the present invention by knowing those skilled in the art The protection domain of the claims in the present invention should all be belonged to.

Claims (9)

1. a kind of method of poor quality gasoline hydrogenation modification, which is characterized in that this approach includes the following steps:
(1) enter pre-hydrogenator after catalytic gasoline is mixed with hydrogen, reacted in the presence of catalyst for pre-hydrogenation, reacted Condition is:1.0~3.0Mpa of hydrogen partial pressure, 100~260 DEG C of reaction temperature, 2.0~8.0h of volume space velocity-1, hydrogen to oil volume ratio 10 ~200v/v;
(2) step (1) product enters in fractionating column, in 0.5~1.0Mpa of tower top pressure, 90~130 DEG C of feeding temperature, tower top temperature 70~110 DEG C of degree, cut at 190~230 DEG C of column bottom temperature it is light, in, heavy gasoline components;
(3) the light petrol component being ejected from fractionation column comes out directly as reformulated gasoline blend component from fractionating column side line Middle gasoline component and hydrogen mixing after enter the first hydrodesulphurisatioreactors reactors, carried out in the presence of mild hydrogenation desulphurization catalyst Reaction, reaction condition are:1.0~3.0Mpa of hydrogen partial pressure, 200~300 DEG C of reaction temperature, 2.0~5.0h of volume space velocity-1, hydrogen Oil volume is returned again to than 200~400v/v, middle gasoline hydrodesulfurizationmethod product in fractionating column;
(4) enter hydro-upgrading reactor after heavy gasoline components and the hydrogen mixing come out from fractionation column bottom, in hydro-upgrading It is reacted in the presence of catalyst, reaction condition is:1.0~3.0Mpa of hydrogen partial pressure, 320~450 DEG C of reaction temperature, volume space velocity 1.0~3.0h-1, 250~500v/v of hydrogen to oil volume ratio;
(5) product of step (4) enters the second hydrodesulphurisatioreactors reactors, is carried out in the presence of catalyst for selectively hydrodesulfurizing anti- It answers, reaction condition is:1.0~3.0Mpa of hydrogen partial pressure, 220~350 DEG C of reaction temperature, 2.0~5.0h of volume space velocity-1, hydrogen oil body 250~500v/v of product ratio;And
(6) after the cooling of step (5) product, gas-liquid separation, the hydrogen come out at the top of product separator are carried out into product separator Enter circulating hydrogen compressor after desulphurization of recycle hydrogen tower desulfurization process to recycle, product separator bottom liquid phases product enters steady Tower is determined, in 0.7~1.2Mpa of tower top pressure, 140~200 DEG C of feeding temperature, 120~180 DEG C of tower top temperature, column bottom temperature 180 Sulfurous gas is removed under the conditions of~240 DEG C, reformulated gasoline product is mixed to get with light petrol.
2. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the pre- hydrogenation catalyst Agent carrier is the mixture of aluminium oxide, silica or both, and active component is one or more of the VIth B, the VIIIth race, by urging Agent weight 100% is counted, and active component oxide content is 10~30%, and surplus is carrier.
3. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the pre- hydrogenation catalyst Agent specific surface area is 100~300m20.2~0.6ml/g of/g, Kong Rongwei.
4. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the mild hydrogenation is de- Sulfur catalyst carrier is the mixture of aluminium oxide and hydrogen type molecular sieve, and active component is one kind or several in the VIth B, the VIIIth race Kind, the molecular sieve is one or more of HZSM-5, HMCM-22, H β and HY, and the molecular sieve accounts for the 10 of catalyst weight ~60%, active component oxide accounts for the 5~15% of catalyst weight.
5. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the mild hydrogenation is de- Sulfur catalyst specific surface area is 200~400m20.4~0.8ml/g of/g, Kong Rongwei.
6. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the hydro-upgrading is urged Agent carrier is the compound of aluminium oxide and molecular sieve, and active component is the VIth B, one or more of the VIIIth race, described point Son sieve is one or more of ZSM-5, Beta, SAPO molecular sieve, in terms of catalyst weight 100%, the molecular sieve content It is 60~90%, the active component oxide content is 1~10%.
7. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the hydro-upgrading is urged Agent specific surface area is 200~500m20.2~0.5ml/g of/g, Kong Rongwei.
8. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the selective hydrogenation Desulphurization catalyst is with Al2O3、SiO2、TiO2And ZrO2One or more of be carrier, with P2O5、K2One kind in O and MgO or Several is auxiliary agent, and active component is one or more of VI B races, VIII race, based on catalyst weight 100%, active component oxygen Compound accounts for 6~20%, and auxiliary agent accounts for 1~15%, and surplus is carrier;The catalyst for selectively hydrodesulfurizing specific surface area is 170 ~270m20.3~0.6ml/g of/g, Kong Rongwei.
9. the method for poor quality gasoline hydrogenation modification according to claim 1, which is characterized in that the catalytic gasoline is Catalytically cracked gasoline, sulfur content are less than or equal to 1000mg/kg, and olefin(e) centent is less than or equal to 45v%.
CN201511027275.5A 2015-12-30 2015-12-30 A kind of method of poor quality gasoline hydrogenation modification Active CN106929098B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201511027275.5A CN106929098B (en) 2015-12-30 2015-12-30 A kind of method of poor quality gasoline hydrogenation modification

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201511027275.5A CN106929098B (en) 2015-12-30 2015-12-30 A kind of method of poor quality gasoline hydrogenation modification

Publications (2)

Publication Number Publication Date
CN106929098A CN106929098A (en) 2017-07-07
CN106929098B true CN106929098B (en) 2018-10-16

Family

ID=59442009

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201511027275.5A Active CN106929098B (en) 2015-12-30 2015-12-30 A kind of method of poor quality gasoline hydrogenation modification

Country Status (1)

Country Link
CN (1) CN106929098B (en)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1597864A (en) * 2003-09-15 2005-03-23 中国石油化工股份有限公司 Process for hydrogenating treatment of foulty gasoline
CN103059955A (en) * 2011-10-21 2013-04-24 中国石油化工股份有限公司 Method for producing clean gasoline from catalytic cracking gasoline
CN104673378A (en) * 2015-02-04 2015-06-03 中国石油大学(北京) Method for producing desulfurized gasoline

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1597864A (en) * 2003-09-15 2005-03-23 中国石油化工股份有限公司 Process for hydrogenating treatment of foulty gasoline
CN103059955A (en) * 2011-10-21 2013-04-24 中国石油化工股份有限公司 Method for producing clean gasoline from catalytic cracking gasoline
CN104673378A (en) * 2015-02-04 2015-06-03 中国石油大学(北京) Method for producing desulfurized gasoline

Also Published As

Publication number Publication date
CN106929098A (en) 2017-07-07

Similar Documents

Publication Publication Date Title
FI127206B2 (en) Process for producing biofuel and biofuel components
CN101245260A (en) Method for producing ultra-low-sulfur oil
CN101597510B (en) Catalyzing distillation method for gasoline alkylate desulfuration
CN106929099B (en) A kind of method of inferior patrol hydro-upgrading
WO2019018224A1 (en) Systems and methods for processing heavy oils by oil upgrading followed by refining
CN103965984A (en) Method for removing mercaptan in liquefied petroleum gas through catalysis
CN104031679A (en) Method for production of olefin and aromatic hydrocarbon from naphtha
CN106147844B (en) A kind of method of hydrotreating for producing super low-sulfur oil
CN104711022A (en) Two-stage catalytic gasoline upgrading method for increasing gasoline yield and producing ultra-low sulfur gasoline
GB2561951A (en) A method for producing a clean gasoline and a system for producing the same
CN102634368A (en) Method for inferior gasoline modification
CN103074104A (en) Gasoline hydro-desulfurization method
CN106929098B (en) A kind of method of poor quality gasoline hydrogenation modification
CN102167985B (en) Hydro-upgrading method for ungraded gasoline
CN101314734B (en) Selective hydrogenation desulfurization method for gasoline
CN103059964B (en) Method for producing ultra-low sulfur gasoline
CN104726132A (en) Process For The Hydrodesulphurization Of Hydrocarbon Cuts
CN103396832A (en) Modification method for full-range catalytic cracking gasoline
CN102634371A (en) Method for gasoline modification
CN107163984B (en) A kind of method of poor ignition quality fuel production high-knock rating gasoline
CN106147838B (en) A kind of method for producing super low-sulfur oil
CN102634370A (en) Method for gasoline hydrogenation modification
CN102399588A (en) Method for reducing sulfur content in sulfur-containing light oil
CN102618328B (en) Gasoline processing method
CN108018079A (en) A kind of method for reducing content of sulfur in gasoline

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant