CN100419045C - Catalysis method for improving quality of gasoline in low quality - Google Patents
Catalysis method for improving quality of gasoline in low quality Download PDFInfo
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- CN100419045C CN100419045C CNB2004100379298A CN200410037929A CN100419045C CN 100419045 C CN100419045 C CN 100419045C CN B2004100379298 A CNB2004100379298 A CN B2004100379298A CN 200410037929 A CN200410037929 A CN 200410037929A CN 100419045 C CN100419045 C CN 100419045C
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Abstract
The present invention relates to a catalyzing and modifying method for low-qualified gasoline. Gasoline raw materials are injected into a dense phase fluidized bed reactor with uniform velocity and contact and react with a catalyst in the fluidized bed reactor, the generated oil mixture is sent to a settler of a catalytic cracking reactor by lifting, and thus, the separation of oil and products is completed.
Description
Technical field
The invention belongs to the catalytic process for modifying of petroleum hydrocarbon under the situation that does not have hydrogen, more particularly, is a kind of method of low-quality gasoline being carried out catalytic reforming
Background technology
In refining of petroleum industry, catalytic cracking process and engineering are one of most important process engineerings.Existing catalytic cracking technology almost all adopts riser reactor and reaction-regeneration system flow process, and its riser tube is generally 25～40 meters long.The stock oil of preheating enters riser reactor through feed nozzle, contact with high temperature catalyst from revivifier, reactions such as stock oil vaporization and generation cracking, the oil gas of entrained catalyst upwards flows along riser tube with certain linear speed (as 10 meter per seconds), the reaction while flowing.Present most 2～3 seconds of the reaction times.The coke generation is constantly arranged in the reaction process and be deposited on catalyst surface, cause activity of such catalysts and selectivity to descend.Oil gas and catalyzer through fast divide device (equipment) to separate after, band Pd/carbon catalyst (reclaimable catalyst) through stripping remove be entrained between the granules of catalyst and the oil gas of granule interior after enter revivifier, coke burning regeneration in the presence of air, catalyzer after the regeneration returns the riser reactor bottom and forms circulation loop, reaction oil gas enters separation system, further isolates various hydrocarbon ils products.Primary first-order equation is unconverted in the raw material reacts for the partial material of light-end products (being commonly referred to recycle stock or turning oil) enters riser reactor once more.The raw material overwhelming majority that catalytic cracking is at present handled is a heavy feed stock, as wax oil, normal pressure and/or vacuum residuum and other inferior raw material, its technical development is except developing the cracking catalyst and auxiliary agent that is fit to various heavys, inferior raw material, existing various heat recuperation technology, more be to carry out various local improvement, reach certain purpose or effect to meet the needs of around riser reactor.Existing main and important new technology and effect thereof comprises:
1. catalytic cracking catalyst and auxiliary agent: reduce green coke and improve the purpose product yield and adapt to the product property requirement, as boosting of octane rating, reduce gasoline olefin and sulphur content, and increasing output of diesel oil, minimizing regenerated flue gas SO
x, NO
xDischarging or the like;
2. heavy oil feed new type nozzle atomization technique improves raw material and catalyzer contact condition, improves the purpose product yield;
3. riser tube exports oil gas isolation technique rapidly and efficiently, reduces cracking;
4. the efficient steam stripping technique of spent agent reduces green coke and loss, improves product yield;
5. highly efficient regeneration technology is burnt, burns new techniques such as jar as two-stage regeneration, fast bed, improve to burn intensity, rapidly and efficiently recovery activity of such catalysts and selectivity;
6. riser tube reaction terminating technology is made terminator with materials such as water, shortens the reaction times, reduces secondary reaction, improves light oil yield;
7. downflow system/upflowing external warmer and interior heat collector and other heat-obtaining facility, the high efficiente callback superfluous heat improves intermingled dregs ratio, cuts down the consumption of energy;
8. other is a new technology just under development as millisecond catalytic cracking, down-flow reactor etc., and purpose is further to shorten the reaction times, reduce the back-mixing of catalyzer in riser tube, further improves product and distributes.Even but adopted above-mentioned various new technology, in the composition of its catalytically cracked gasoline, olefin(e) centent is 40～70% still generally, adopt new technology or raw catalyst after olefin(e) centent also generally be not less than 20%, and sulphur content is generally 2～20% of feed sulphur content.
Along with the increasingly stringent of legislations of environmental protection, the quality of gasoline index is also strict day by day.Requirement to the quality of gasoline standard is vapour pressure, sulphur, nitrogen, alkene and the aromatic hydrocarbons (benzene) of restriction gasoline both at home and abroad, and the gasoline quality standard of countries in the world has certain difference on specific targets.China is alkene ≯ 30%, sulphur ≯ 800ppm to commercial gasoline in the requirement aspect alkene, the sulphur at present.
CN1232069A discloses a kind of catalysis conversion method of producing Trimethylmethane and being rich in isoparaffin gasoline.This method is that stock oil and hot regenerated catalyst in the bottom of riser reactor cracking reaction are taken place, the oil gas and the carbon-bearing catalyzer that generate are up, under the certain reaction environment, carry out hydrogen transfer reactions and isomerization reaction, Trimethylmethane in the products therefrom in the liquefied gas is 20～40 heavy %, isoparaffin is 30～45 heavy % in the gasoline, alkene can reach below the 30 heavy %, and the RON of gasoline, MON are respectively 90～93 and 80～84.This method has reduced gasoline olefin, but diesel yield decline is more.
CN1244568A discloses a kind of catalysis conversion method of producing low-alkene gasoline and high-yield diesel oil.This method is that the regenerated catalyst with stock oil and heat contact at reactor lower part the macromole cracking reaction takes place, the oil gas of generation and be with that Pd/carbon catalyst is up proceeds cracking reaction, hydrogen transfer reactions and isomerization reaction in a bed reactor.Reaction product is separated with spent agent, and spent agent recycles after regeneration, and reaction product is further separated.This method gasoline olefin is below 28 heavy %.
CN1303909A and CN1244569A then disclose the catalysis conversion method that reduces gasoline olefin, sulphur, nitrogen, and in fact this method and CN1244568A are similar.The common trait of these three kinds of methods has been to adopt riser tube to add the method for bed reactor, this will cause the investment cost transformed with new device very big, and because gasoline upgrading has adopted identical catalyst recirculation amount with cracking heavy feedstocks, therefore seeming for gasoline upgrading is not very flexible.
CN1325941A also discloses a kind of FCC gasoline modifying method.This method is carried out in former riser tube, contact the volume processing power that makes gasoline upgrading, this method can influence former riser reactor with pentacyclic mesopore zeolite by making raw material in riser tube, and how unknown actual effect is.
CN2380297Y discloses a kind of catalysis conversion method that adopts duo-lift tube reactor, and wherein to keep former catalytic cracking process process constant for riser tube, and another root riser tube carries out gasoline upgrading.The major technique characteristics of this method are to have adopted the two-part riser tube, and constitute the two-way circulation of catalyzer with regeneration system rapidly, make two sections series connection of reaction oil gas, the relay of catalyzer two-way.Regulate flexible characteristic though this method has the catalyst recirculation amount, shortcoming is also fairly obvious: reaction pressure is difficult to steady control, and the actually operating difficulty is big, investment is also bigger, and product distributes also not satisfactory in addition.
CN2510151Y discloses a kind of catalysis conversion method of employing three riser reactors, two riser tube chargings respectively, and then enter the 3rd riser tube.This method is in fact than more difficult realization of double lifting leg and operation, and investment is bigger, sees almost do not have any practical significance in present stage.
Above catalytic reforming process is all carried out in conventional catalyst cracking reaction district, adopts double lifting leg or three riser tube technologies, has charging distinguishing feature flexibly, and difficulty is bigger but device operates, and gas is on the high side in the product distribution.And adopt riser tube to add the technology of bed reactor, and though product distributes and improves relatively, operation easier is also less, and construction investment is big, and gasoline upgrading is dumb, and influences the heavy oil processing power of device.
In sum, though disclose many gasoline catalyzing method for modifying in the prior art, but problem such as these methods ubiquity engineering amount of reform in implementation process is big or operation easier is big, and the fall of content of olefin in gasoline is limited behind the upgrading, is difficult to satisfy the environmental regulation requirement of increasingly stringent.
Summary of the invention
The purpose of this invention is to provide a kind of method of low-quality gasoline being carried out catalytic reforming, so that when reducing foreign matter contents such as content of olefin in gasoline and sulphur, nitrogen, do not influence of the processing of former FCC conversion zone to various raw materials, also can not influence the heavy oil conversion performance of device, and it is simple to have engineering construction, gasoline upgrading is versatile and flexible, the product characteristics preferably that distribute.
Method provided by the invention is: gasoline stocks injects at the uniform velocity fluidized-bed reactor of close phase, contacts, reacts with catalyzer in it, and the finish mixture that is generated is delivered in the catalyst cracker settling vessel through promoting, and finishes finish and separates and product separation.
Compared with prior art, beneficial effect of the present invention is mainly reflected in following aspect:
1, the present invention with close phase at the uniform velocity fluidized-bed reactor carry out successive reaction, reprocessing cycle operating method to reduce gasoline olefin, sulphur, nitrogen content.
2, the manageable raw material ratio of the present invention is more flexible, both can be the high catalytic gasoline of olefin(e) centent, also can be other low-quality gasoline such as gasoline such as coking, straight run, can also be non-gasoline fraction, as poor ignition quality fuel or heavy oil.
3, catalyst system therefor of the present invention both can be the catalyzer and the auxiliary agent of existing catalytic cracking, also can be new catalyzer or auxiliary agent such as gasoline desulphurization sorbent with some specific function, fall alkene auxiliary agent etc.
The yield of purpose product was higher when 4, the present invention was to gasoline upgrading, liquid yield 〉=96%, coke %≤1.5%, dry gas %≤1%.
5, the present invention can play the double effects that not only falls alkene but also fall sulphur, nitrogen, and wherein alkene can drop to below the 10v%, and sulphur reduces 20-90%, and nitrogen content reduces more than 90%.In addition, aromatic hydrocarbons and isoparaffin content are higher in the gasoline, so octane value is constant substantially.
6, the present invention and existing catalytic cracking unit are got in touch very closely at aspects such as Btu utilization and catalyst regeneration, product separation, are newly-built or reconstruct close phase at the uniform velocity fluidized-bed reactor and/or upper reaches or downflow system external warmer.
7, compare with double lifting leg or MIP technology, implement when of the present invention newly-built or with the obvious advantage when transforming: the reactor absolute altitude is lower, and construction cost is few and more convenient; The reactor use temperature is low, no particular requirement, and gross investment is low; In addition, the going into operation and processing ease of this reactor, and, because this reactor application aims is strong, catalyzer or auxiliary agent can be earlier in this reactor with higher activity or concentration (reserve) and the material reaction that needs upgrading, so catalyzer or auxiliary agent consumption are lower, better effects if.
Embodiment
Gasoline stocks of the present invention is selected from: the mixture of one or more in straight-run spirit, coker gasoline, viscosity breaking gasoline, catalytic cracking raw gasline, catalytic cracking stable gasoline and other oil refining or the gasoline fraction that chemical process generated.Described gasoline stocks both can be full distillation gasoline, also can be part narrow fraction gasoline, for example, and the gasoline fraction of initial boiling point-120 ℃.The olefin(e) centent of described gasoline fraction can be the heavy % of 20-70, and its sulphur content can be the 2-20% of FCC feed sulphur content.
The catalyzer that the present invention was suitable for can be that active ingredient is selected from one or more in Y or HY type zeolite, the USY that contains or do not contain rare earth, the ZSM-5 series zeolite that contains or do not contain rare earth or the supersiliceous zeolite with five-membered ring structure, β zeolite, the ferrierite, it also can be the amorphous silicon aluminium catalyzer, and various FCC auxiliary agents, as reducing the gasoline olefin auxiliary agent, falling sulfur absorbent, propylene enhancing auxiliary agent etc.
Close phase of the present invention is the apparent bed density 〉=100Kg/m of fluidized-bed reactor inner catalyst at the uniform velocity
3, preferred apparent bed density is 150-500Kg/m
3This close phase is the interior linear speed≤10m/s of fluidized-bed reactor at the uniform velocity, and preferred linear speed is 0.5-5m/s.It is constant substantially that the linear speed of this reactor outlet and inlet preferably keeps, for example, close phase at the uniform velocity the difference of fluidized-bed reactor outlet and inlet linear speed≤± 0.5m/s, preferred≤+ 0.2m/s, most preferably≤0.1m/s.
The present invention passes in and out the at the uniform velocity difference of the mode of fluidized-bed reactor of close phase according to catalyzer, and this reactor is divided into the at the uniform velocity close fluidized-bed two big classes at the uniform velocity mutually of fluidized-bed and upflowing of the close phase of downflow system.The close phase of downflow system at the uniform velocity fluidized-bed reactor is defined as: catalyzer enters from reactor top, flows out from reactor lower part.The close phase of upflowing at the uniform velocity fluidized-bed reactor is defined as: catalyzer enters from reactor lower part, flows out from reactor top.
Further specify method provided by the invention below in conjunction with concrete embodiment, but therefore the present invention is not subjected to any limitation.
One of embodiment (downflow system): for the catalytic cracking unit of existing band external warmer (upflowing or downflow system), newly establish at the uniform velocity fluidized-bed reactor of a close phase of downflow system, catalyzer is taken out from external warmer, enter the top of newly-increased downflow reactor, and contact, react with gasoline stocks in injecting this reactor.Reaction oil gas flows downward with a constant linear speed (as 0.5m/s) limit coronite with mixture of catalysts, and the bed apparent density of this reactor is controlled at 300Kg/m
3Carbon-bearing catalyzer and reaction product are left from reactor bottom together with the linear speed of 0.5m/s, enter FCC reactor settling vessel and separate.
Two (downflow systems) of embodiment: newly-built or reconstruction downflow system external warmer is an at the uniform velocity fluidized-bed reactor (reactor and heat collector unite two into one) of close phase.Gasoline stocks injects this reactor and contacts, reacts with catalyzer in the reactor.The bed apparent density of reactor is 100Kg/m
3More than.The mixture of catalyzer and reaction oil gas flows downward with constant linear speed limit coronite together.Carbon-bearing catalyzer and reaction product enter settling vessel and separate to leave from reactor bottom with the essentially identical linear speed of inlet.
Three (upflowings) of embodiment: newly-built or to reconstruct existing upflowing external warmer be at the uniform velocity fluidized-bed reactor (reactor and heat collector unite two into one) of close phase of the present invention.Gasoline stocks and catalyzer enter from reactor bottom.The inlet linear speed is 1m/s, and the reactor bed apparent density is 250Kg/m
3More than.Reaction oil gas and the carbon-bearing catalyzer linear speed about with 1m/s leaves the top of reactor, enters settling vessel and separates.
Four (upflowings) of embodiment: for the catalytic cracking unit of existing band external warmer (upflowing or downflow system), a newly-increased close phase is fluidized-bed reactor at the uniform velocity, catalyzer takes out from external warmer and enters the at the uniform velocity bottom of fluidized-bed reactor of new density phase, injects gasoline stocks.Catalyzer and reaction product in newly-increased dense bed reactor head after cyclone separator (as horizontal) separates, reaction oil gas enters later separation and absorption-stable system, the carbon-bearing catalyzer is direct or return revivifier behind stripping, and the riser tube bottom that also can directly enter original device comes along reaction with regenerator.
Five (going up or downflow system) of embodiment: a newly-increased close phase is fluidized-bed reactor at the uniform velocity, catalyzer takes out from the catalyzer storage tank (live catalyst and/or equilibrium catalyst) of existing catalytic unit and/or the small-sized charging system of catalyzer automatic or manual and/or heat collector and/or revivifier and enters the at the uniform velocity end of fluidized-bed reactor (or top) portion of this close phase, injects gasoline stocks.Catalyzer and reaction product in this reactor head (or end) after cyclone separator (as horizontal) separates, reaction oil gas enters the stripping tower that separation column is newly-built or reconstruct, the carbon-bearing catalyzer is direct or return revivifier behind stripping, and the riser tube bottom that also can directly enter original device comes along reaction with regenerator.
The method of the invention can be described in detail as follows: the gasoline stocks of preheating or not preheating enters close phase and at the uniform velocity contacts, reacts with catalyzer in the fluidized-bed reactor, and the linear speed of reactor outlet and inlet is constant substantially, as is controlled at 0.2～1.5m/s.Gasoline stocks is 100～600 ℃ in temperature of reaction, is preferably 120～5 00 ℃, and reaction pressure 0.05～0.40MPa is preferably 0.1～0.25MPa, and weight hourly space velocity is 1～150h
-1, be preferably 2～100h
-1The weight ratio of catalyzer and gasoline is 1～40: 1, be preferably 3～25: 1, the weight ratio of water vapour and stock oil is 0～0.2: 1, be preferably 0.05～0.1: advance hydrogen transference and reactions such as isomerization, aromizing under 1 the condition, reaction product is delivered in the FCC apparatus reactor settling vessel with the mixture of water vapour and band Pd/carbon catalyst and is separated, and reaction product isolated obtains dry gas, liquefied gas, gasoline and diesel oil.Wherein liquefied gas is rich in alkene and Trimethylmethane, and the alkene of gasoline is very low, but isomeric hydrocarbon alkane and aromatic hydrocarbons are higher.Spent agent enters revivifier through stripping, and the catalyzer after the regeneration returns reaction cycle and uses.
The present invention is further illustrated below in conjunction with embodiment, but therefore the present invention is not subjected to any restriction.The character of used stock oil and catalyzer sees Table 1 and table 2 among the embodiment.
Embodiment 1
Present embodiment explanation: adopt method provided by the invention, different sources gasoline is carried out the result of catalyzed conversion.
With table 1 listed stock oil and the listed catalyzer 2 (CAT2) of table 2, at the uniform velocity carry out the catalytic reforming experiment in the fluidized-bed reactor in the small-sized close phase of successive reaction-regenerated.Enter after gasoline stocks and high-temperature water vapor mix close mutually at the uniform velocity in the fluidized-bed reactor with the catalyzer contact reacts.Reaction product, steam and reclaimable catalyst separate in settling vessel, and reaction product further is separated into gas and liquid, and reclaimable catalyst enters revivifier and burns behind stripping, and regeneration is finished rear catalyst and recycled.
Table 3 is experiment condition, experimental result and gasoline property.By table 3 as seen, the different sources gasoline sample is behind catalytic reforming, and olefin(e) centent is reduced to below the 10v%, and sulphur content reduces 50-90%, and nitrogen content drops to 1-14ppm, and the aromatic hydrocarbons of gasoline and isoparaffin increase are more, and the octane value of gasoline is constant substantially.
Embodiment 2
Present embodiment explanation: adopt method provided by the invention, use the catalyzed conversion effect of dissimilar catalyzer.
With table 1 listed stock oil 1 and the listed catalyzer of table 2, at the uniform velocity carry out the catalytic reforming experiment in the fluidized-bed reactor in the small-sized close phase of successive reaction-regenerated.Enter in this reactor after gasoline stocks and high-temperature water vapor mix and the catalyzer contact reacts.Reaction product, steam and reclaimable catalyst separate in settling vessel, and reaction product further is separated into gas and liquid, and reclaimable catalyst enters revivifier and burns behind stripping, and the catalyst recirculation after regeneration is finished is used.
Table 4 is experiment condition, experimental result and gasoline property.By table 4 as seen, same raw material effect behind dissimilar catalyst upgradings has certain difference.Olefin(e) centent is reduced to below the 10v%, and sulphur content drops to below the 600ppm, and nitrogen content drops to below the 1.5ppm, and the aromatic hydrocarbons of gasoline and isoparaffin are more, is that the octane value of gasoline is constant substantially more than the 30 heavy %.
Embodiment 3
Present embodiment explanation: adopt method provided by the invention, the catalyzed conversion effect of gasoline stocks under the different operating condition.
With table 1 listed stock oil 3 and the listed catalyzer 1 of table 2, at the uniform velocity carry out the catalytic reforming experiment in the fluidized-bed reactor in the small-sized close phase of successive reaction-regenerated.Enter in this reactor after gasoline stocks and high-temperature water vapor mix and the catalyzer contact reacts, temperature of reaction is 250-550 ℃.Reaction product, steam and reclaimable catalyst separate in settling vessel, and reaction product further is separated into gas and liquid, and reclaimable catalyst enters revivifier and burns behind stripping, and the catalyst recirculation after regeneration is finished is used.
Table 5 is experiment condition, experimental result and gasoline property.By table 5 as seen, the different operating condition has certain difference to the effect of gasoline catalyzing upgrading.Be reduced to below the 10v% through content of olefin in gasoline behind the catalytic reforming generally, sulphur content drops to below the 1000ppm, and nitrogen content drops to below the 14ppm, and the aromatic hydrocarbons of gasoline and isoparaffin are more, be respectively 30 heavy % and 47 and weigh more than the %, the octane value of gasoline descends few.
Embodiment 4
Present embodiment explanation: adopt method provided by the invention, to catalytic gasoline in the medium-sized close phase catalyzed conversion effect in the fluidized-bed reactor at the uniform velocity.
With table 1 listed stock oil and the listed catalyzer of table 2, at the uniform velocity carry out the catalytic reforming experiment in the fluidized-bed reactor in the medium-sized close phase of successive reaction-regenerated.Medium-sized close phase at the uniform velocity fluidized-bed reactor by conventional riser fluid catalytic cracking transformation is built up.In newly-built experimental installation, not charging of riser tube only plays the catalyst channels effect.
Enter after gasoline stocks and high-temperature water vapor mix close mutually at the uniform velocity in the fluidized-bed reactor with the catalyzer contact reacts, the reactor bed apparent density is 260Kg/m
3, the catalyzer linear speed is 1m/s.Reaction product, steam and reclaimable catalyst separate in settling vessel, and reaction product further is separated into gas and liquid, and reclaimable catalyst enters revivifier and burns behind stripping, and regeneration is finished rear catalyst and recycled.
Table 6 is experiment condition, experimental result and gasoline property.By table 6 as seen, gasoline sample is through medium-sized close phase at the uniform velocity behind the fluid bed reactor catalysis upgrading, olefin(e) centent is reduced to below the 10v%, sulphur content drops to below the 350ppm, nitrogen content drops to below the 3ppm, and the aromatic hydrocarbons of gasoline and isoparaffin are more, are respectively 34 heavy % and 42 and weigh more than the %, and the octane value of gasoline descends few.
Table 1
Table 2
Table 3
Table 4
Table 5
Table 6
Claims (10)
1. low-quality gasoline catalyzing method for modifying, it is characterized in that: gasoline stocks injects at the uniform velocity fluidized-bed reactor of close phase, contact, react with the catalyzer in it, the finish mixture that is generated is through promoting, deliver in the catalyst cracker settling vessel, finishing finish separates and product separation, described catalyzer is that active ingredient is selected from one or more catalyzer in the Y that contains or do not contain rare earth or HY type zeolite, the USY zeolite that contains or do not contain rare earth, β zeolite, the ferrierite, or amorphous silicon aluminium catalyzer, and various FCC auxiliary agent.
2. according to the method for claim 1, it is characterized in that being selected from: one or more in straight-run spirit, coker gasoline, viscosity breaking gasoline, catalytic cracking raw gasline, catalytic cracking stable gasoline and other oil refining or the gasoline fraction that chemical process generated at described gasoline stocks.
3. according to the method for claim 1, it is characterized in that the at the uniform velocity apparent bed density 〉=100Kg/m of fluidized-bed reactor inner catalyst of described close phase
3
4. according to the method for claim 3, it is characterized in that described close phase at the uniform velocity the apparent bed density of fluidized-bed reactor inner catalyst be 150-500Kg/m
3
5. according to the method for claim 1, it is characterized in that the at the uniform velocity interior linear speed≤10m/s of fluidized-bed reactor of described close phase, and the difference of this reactor outlet and inlet linear speed is ± 0.5m/s.
6. according to the method for claim 5, it is characterized in that described close phase at the uniform velocity the linear speed in the fluidized-bed reactor be 0.5-5m/s, and the difference of this reactor outlet and inlet linear speed is ± 0.2m/s.
7. according to the method for claim 6, it is characterized in that described close phase at the uniform velocity fluidized-bed reactor outlet and inlet linear speed≤0.1m/s.
8. according to the method for claim 1, it is characterized in that described close phase at the uniform velocity fluidized-bed reactor be at the uniform velocity fluidized-bed or the close phase of upflowing fluidized-bed at the uniform velocity of the close phase of downflow system.
9. according to the method for claim 1, it is characterized in that the catalytic reforming condition of described gasoline stocks is: temperature of reaction 100-600 ℃, reaction pressure 0.05-0.40Mpa, weight hourly space velocity are 1-150h
-1, catalyzer and gasoline stocks weight ratio be 1-40: 1, the weight ratio of water vapour and gasoline stocks is 0-0.2: 1.
10. according to the method for claim 9, it is characterized in that the catalytic reforming condition of described gasoline stocks is: temperature of reaction 120-500 ℃, reaction pressure 0.1-0.25Mpa, weight hourly space velocity 2-100h
-1, catalyzer and gasoline stocks weight ratio be 3-25: 1, the weight ratio 0.05-0.1 of water vapour and gasoline stocks: 1.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5171426A (en) * | 1991-04-01 | 1992-12-15 | Texaco Inc. | Control method for solvent refining lubricating oils |
| CN1278291A (en) * | 1997-09-03 | 2000-12-27 | Hfm国际公司 | Aromatics separation process and method of retrofitting existing equipment for same |
| CN1325941A (en) * | 2000-05-31 | 2001-12-12 | 中国石油化工集团公司 | Process for modifying catalytically cracked gasoline |
-
2004
- 2004-05-14 CN CNB2004100379298A patent/CN100419045C/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5171426A (en) * | 1991-04-01 | 1992-12-15 | Texaco Inc. | Control method for solvent refining lubricating oils |
| CN1278291A (en) * | 1997-09-03 | 2000-12-27 | Hfm国际公司 | Aromatics separation process and method of retrofitting existing equipment for same |
| CN1325941A (en) * | 2000-05-31 | 2001-12-12 | 中国石油化工集团公司 | Process for modifying catalytically cracked gasoline |
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