CN101870632A - Method for producing low-carbon olefin - Google Patents
Method for producing low-carbon olefin Download PDFInfo
- Publication number
- CN101870632A CN101870632A CN200910082941A CN200910082941A CN101870632A CN 101870632 A CN101870632 A CN 101870632A CN 200910082941 A CN200910082941 A CN 200910082941A CN 200910082941 A CN200910082941 A CN 200910082941A CN 101870632 A CN101870632 A CN 101870632A
- Authority
- CN
- China
- Prior art keywords
- reactor
- hydrogen
- catalyst
- dehydrogenation
- olefin
- 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.)
- Pending
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention discloses a method for producing low-carbon olefin by petroleum hydrocarbon. The method comprises the following steps: taking C4-C35 petroleum hydrocarbon as a raw material; dehydrogenizing in the presence of a dehydrogenation catalyst to obtain unsaturated petroleum hydrocarbon and hydrogen; leading the hydrogen to carry out combustion reaction with externally supplementary oxygen under the action of a hydrogen combustion catalyst so as to heat a material flow to a reaction temperature for olefin conversion; taking water vapor simultaneously generated from combustion as a diluent for olefin conversion; leading the unsaturated petroleum hydrocarbon to carry out olefin conversion at the presence of the catalyst so as to transform high-carbon olefin into the low-carbon olefins such as C2, C3, C4 and the like; and finally separating the low-carbon olefins to obtain ethylene, propylene, butylene, bivinyl and the like.
Description
Technical field
The present invention relates to a kind of method of producing low-carbon alkene, more particularly, relate to a kind of method of producing low-carbon alkene by petroleum hydrocarbon.
Background technology
As everyone knows, be a strong endothermic process of high temperature by petroleum hydrocarbon through producing low-carbon olefins by cracking.The method that present modal oil stable hydrocarbon is produced low-carbon alkene such as ethene, propylene and divinyl etc. is a steam splitting process.About in the world 99% ethene and 50% above propylene are produced by this method.Because steam cracking method production is operated at present in very harsh conditions, for example the temperature in latter stage of crack furnance radiation section furnace tube reaches or surpasses 1125 ℃, and the residence time of material in radiant coil shortens to 0.2s even shorter.Therefore under existing state of the art, the improved possibility that oil stable hydrocarbon steam cracking method is produced low-carbon alkenes such as ethene, propylene and divinyl is very little.In light of this situation, studying the fixed-bed catalytic cracking technique that is applicable to petroleum naphtha at present, as CN02129551, CN1380898A, CN200510028797, CN03141148.With respect to the steam heat cracking, because the existence of catalyzer not only can reduce cracking temperature, and can improve the selectivity of low-carbon alkene, thereby be subjected to paying attention to widely.But the uneven shortcoming of reaction temperature profile that solid catalyst adding reaction tubes and the strong endothermic character of cracking process are caused becomes a difficult problem in the evolution of fixed-bed catalytic cracking technique.
As seen, because the strong endothermic character of high temperature of petroleum hydrocarbon cracking process, the steam heat cracking technology of existing industrial employing and Deep Catalytic Cracking process process just under study for action are faced with respectively because outside indirect heating mode causes the huge energy demand and the even problem of temperature distributing disproportionation of ultrahigh-temperature.In order to continue to promote the development that petroleum hydrocarbon transforms preparation low-carbon alkene technology, still needing to provide a kind of is the raw material production low-carbon alkene with the oil stable hydrocarbon, the method that the while energy consumption reduces significantly.
Transform preparation low-carbon alkene aspect from petroleum hydrocarbon, what cause concern is the carbon four and the above olefins by catalytic cracking producing light olefins technology of fast development in recent years.Comprise with the LURGI being fixed-bed process (the Producing Propylene from Low Valued Olefins.Hydroca rbon Eng of representative, 1999,5 (4): 66～68 and Increase propylene yield cost-effectively, Hydrocarbon Processing, 2002,81 (12): 77～80) with KBR company is fluidized-bed process (the Producing propylene of representative, Hydrocarbon Engineering, 2004,9 (7): 69～72 and Consider Improving Refining and Petrochemical Integration as a Revenue-Generating Option.Hydrocarbon Process, 2001,80 (11): 47～53).The fact based on carbon four and the fast development of above olefins by catalytic cracking preparing ethylene and propylene technology, if can change into the petroleum hydrocarbon that mainly consists of saturated hydrocarbons with carbon number alkene, and then utilize carbon four and above olefins by catalytic cracking preparing ethylene and propylene technology to prepare low-carbon alkenes such as ethylene, propylene, will be the route by petroleum hydrocarbon production low-carbon alkene of a novelty undoubtedly.
There have been many companies that industrialized dehydrating alkanes technology can be provided at present in the world.For example relevant patents such as CN1037667C, CN1069226C, CN1013361B, CN1084224C are concentrated and to have been reported by low-carbon alkanes (carbon four and following) and long chain alkane (carbon 12 and more than) dehydrogenation and prepare the technological process of alkene and catalyzer accordingly.From these patents as seen, though use the carbon number difference of raw material hydro carbons, the catalyzer that uses belongs to carrier-precious metal type catalyzer substantially, thereby the proof petroleum hydrocarbon is feasible through the process that dehydrogenation reaction produces with carbon number alkene.Moreover, when the raw material of processing was identical, the energy requirement that produces the certain embodiments of same carbon number alkene will be well below the energy requirement that produces low-carbon alkene cracking process such as ethene, propylene.
Produce with carbon number alkene in petroleum hydrocarbon dehydrogenation set forth above, produce in the technological process of low-carbon alkenes such as ethene, propylene then by olefin cracking, to comprise a certain amount of hydrogen in the logistics after the dehydrogenation, if can under the situation that hydrocarbon material flow exists, change into water to the hydrogen in the mixture flow as thinner, certain energy is provided simultaneously, will will promote significant through the energy supply and the economic worth of dehydrogenation and olefin cracking preparing low carbon olefin hydrocarbon to the petroleum hydrocarbon that the application proposes undoubtedly.
The relevant technology that hydrogen in the mixture flow is changed into water under the situation that hydrocarbon material flow exists can be with reference to SMART vinylbenzene technology.Patent such as US4812597, US4914249 is described this technology: adopt with selective hydrogen burning catalyst and make hydrogen selective combustion under the situation that hydrocarbon species such as ethyl benzene/styrene exist in the logistics of part dehydrogenation afterreaction, the energy that utilizes hydrogen burning to produce is brought up to the temperature of logistics temperature (the about 600 ℃) dehydrogenation once more that dehydrogenation reaction can take place in direct-fired mode.
The application transforms methane content is low in the low and product of producing light olefins Technology Energy demand advantage and hydrogen burning in the advantage of energy aspect providing in conjunction with the petroleum hydrocarbon multistep processes, has proposed the technological process that a kind of new petroleum hydrocarbon transforms producing light olefins.
Summary of the invention
The purpose of this invention is to provide a kind of complete different steam cracking traditional technologys with the method for petroleum hydrocarbon as the raw material production low-carbon alkene.
Concrete, the method for production low-carbon alkene of the present invention comprises the following steps:
(1) dehydrogenation: petroleum hydrocarbon raw material is sent into dehydrogenation reactor, in the presence of dehydrogenation catalyst dehydrogenation reaction takes place, obtain containing the logistics of hydrogen and unsaturated hydrocarbons compounds, described petroleum hydrocarbon raw material is for being selected from C
4～C
35The hydrocarbon mixture of hydrocarbon;
(2) hydrogen burning: the hydrogen burning reactor is introduced in the logistics that contains hydrogen and unsaturated hydrocarbons compounds that step (1) obtains, in the presence of hydrogen burning catalyst, hydrogen in the described logistics and the outside oxygen generation combustion reactions of supplying with, the petroleum hydrocarbon material is heated to the temperature that olefin catalytic transforms, obtains the unsaturated hydro carbons mixture of moisture vapor;
(3) conversion of olefines: the unsaturated hydro carbons mixture of the moisture vapor that step (2) is obtained is introduced olefin reactor, carries out olefin reaction in the presence of the conversion of olefines catalyzer, obtains containing C
2～C
4The logistics of alkene;
(4) separate: contain C what step (3) obtained
2～C
4The logistics of alkene is introduced separation circuit and is separated, and obtains being rich in C
2The product of alkene, be rich in C
3The product of alkene and be rich in C
4The product of alkene.
Preferably, in described step (2), the described logistics that contains hydrogen and unsaturated hydrocarbons compounds is introduced described hydrogen burning reactor with thinner, in the presence of hydrogen burning catalyst, hydrogen and the outside oxygen generation combustion reactions of supplying with;
In step (3), enter that olefin(e) centent is not higher than 50% in the logistics of olefin reactor, preferably be not higher than 35%, more preferably no higher than 20%.
In described step (2), described thinner can be any thinner commonly used, is preferably water vapor.
Preferably, in described step (4), described separation circuit comprises compression, rectifying, extraction and low temperature separation process process.
Preferably, in described step (4), obtain ethylene product, propylene product, butylene product and product butadiene by separation.
Preferably, described dehydrogenation reactor is for adding the fixed-bed reactor or the fluidized-bed reactor of dehydrogenation catalyst, described hydrogen burning reactor is for adding the fixed-bed reactor or the fluidized-bed reactor of hydrogen burning catalyst, and described olefin reactor is for adding the fixed-bed reactor or the fluidized-bed reactor of conversion of olefines catalyzer.
Preferably, described dehydrogenation reactor is the fixed-bed reactor that add dehydrogenation catalyst, described hydrogen burning reactor is for adding the fixed-bed reactor of hydrogen burning catalyst, and described olefin reactor is to add the fixed-bed reactor of conversion of olefines catalyzer.
Preferably, it is dehydrogenation catalyst or nickel catalyst that described dehydrogenation catalyst is selected from carried noble metal Pt, and described hydrogen burning catalyst is selected from carried noble metal Pt or Pd is a hydrogen burning catalyst; Described conversion of olefines catalyzer is one or more the mixture in modification or unmodified ZSM-5, ZSM-11, ZSM-23, MCM-22 and the SAPO molecular sieve catalysts.
Preferably, described petroleum hydrocarbon raw material is one or more the mixture in petroleum naphtha, diesel oil, whiteruss, solid paraffin, normal paraffin mixture, hydrogenation tail oil, tops and the reformate.
Preferably in described step 1), described petroleum hydrocarbon raw material is introduced described dehydrogenation reactor with thinner, in described dehydrogenation reactor, contact, dehydrogenation reaction takes place with dehydrogenation catalyst; In described step 2) in, the described logistics that contains the petroleum hydrocarbon of unsaturated hydrocarbons compounds is introduced described olefin reactor with thinner, in described olefin reactor, contact, the reaction of the conversion of olefines of carbonatoms reduction takes place with the conversion of olefines catalyzer.
Described thinner is introduced reactor after can introducing and mixing in the mixing tank again; Also can directly mix the back and introduce reactor.
Preferred described thinner is selected from a kind of in water vapor and the hydrogen; More preferably wherein dehydrogenation reaction is used the water vapour that generates behind hydrogen and the combustion of hydrogen, and olefin reaction uses water vapor as thinner.
The logistics of the petroleum hydrocarbon that comprises the unsaturated hydrocarbons compounds that obtains in described step (1) generally also comprises the hydro carbons of unreacted stable hydrocarbon, hydrogen and the low carbon number of a spot of carbon below four.Because generally, petroleum hydrocarbon carries out dehydrogenation reaction dehydrogenation reaction mainly takes place, rare carbon-carbon bond cleavage reaction, and therefore, the carbon courtyard base in the carbon courtyard number of described unsaturated hydrocarbons and the raw material is identical.
Preferably carry out temperature of reaction 〉=400 ℃ of conversion of olefines.
Described olefin reaction mainly is that the alkene of macromole number (carbon number 〉=4) scission of link is generated micromolecular alkene (carbon number≤4).
In concrete enforcement of the present invention, the hydrogen that described dehydrogenation reaction generates can be as the heating thermal source.
In the specific implementation process of method of the present invention, adopt De-hydrogen Technology of the prior art, the hydrocarbon compound more than 50% can carry out dehydrogenation reaction in the petroleum hydrocarbon raw material usually.Because the selection of the degree of dehydrogenation reaction and dehydrogenation catalyst, reaction conditions has very big relation, therefore can control the degree of dehydrogenation reaction by selecting different dehydrogenation catalyst and reaction conditions.In the method for the invention, do not limit the degree of dehydrogenation reaction.If only have the hydrocarbon compound below 30% not carry out dehydrogenation reaction in the petroleum hydrocarbon raw material, then in concrete enforcement, can not separate, unreacted stable hydrocarbon can be used as the thinner of olefin reaction, alleviates the coking of reactor.
Preferably the logistics that is rich in stable hydrocarbon that described separation is obtained is returned as raw material, introduces dehydrogenation reactor with described petroleum hydrocarbon raw material.
In all embodiments of the present invention, preferably with the described logistics of carrying out olefin reaction with after dilution steam generation mixes, introduce described olefin reactor.
In described step (3), described conversion of olefines comprises that the identical alkene that conversion of olefines and carbon-to-carbon rupture took place of carbonatoms decomposes.
In described step (4), described separation circuit comprises compression, rectifying, extraction.In concrete enforcement, can be according to raw material variation ranges different in the low-carbon alkene product, in separating device, extract respectively or method such as rectifying, obtain the target product that needs.Promptly the composition and the ratio of basis low-carbon alkene are wherein selected suitable separation process.
In described step (4), will comprise C
2～C
4The logistics of alkene separates, and obtains being rich in C
2～C
4The logistics of alkene and comprise C
4The logistics of above heavy constituent; With the described C that is rich in
2～C
4The logistics of alkene further separates, and obtains ethene, propylene, butylene and product butadiene respectively.
In concrete enforcement of the present invention, can adopt corresponding separating technology according to actual needs, obtain the product of different sizes such as polymerization-grade or chemical grade.
Dehydrogenation catalyst and the conversion of olefines catalyzer that use this area of the prior art may be used to method of the present invention.The DEH series dehydrogenation catalyst of Uop Inc. of introducing as " Liaoning chemical industry " (1992, the 5th phase, p16～19), its main component is that aluminum oxide is a carrier, and Pt is an active ingredient, and Sn/Li is a coagent.Dehydrogenation reaction is usually at 300～700 ℃, preferred 400～600 ℃, and reaction pressure is to carry out under 0～1000kPa, the preferred 0～300kPa.The weight hourly space velocity of described petroleum hydrocarbon raw material can be 0.5～30h
-1, preferred 1～10h
-1Dehydrogenation catalyst is made up of precious metals pt and alumina catalyst support or ZSM-5 molecular sieve, for example the BDH catalyzer produced of Beijing Chemical Research Institute.
The temperature of reaction of olefin cracking is not less than 400 ℃, preferred 500 ℃～600 ℃, more preferably 500～550 ℃; Reaction pressure is 0.05～0.5MPa, preferred 0.05～0.2MPa; The weight hourly space velocity is 1.0～30h
-1, preferred 1.5～20h
-1, comprise the combination of above-mentioned scope.Olefin cracking catalyzer of the prior art comprises with the silicon oxide being carrier, ZSM-5 and ZRP are active ingredient, be the catalyzer of auxiliary agent with elements such as Mo, Ni, Ca, Mg, Ce, P, Re, Pt respectively, temperature of reaction is at 400～550 ℃, reaction pressure 0.1～1.0MPa.Can be referring to " petrochemical complex " (2005, the 34th volume, the 6th phase, p315～319), " Industrial Catalysis " (2004, October, the 12nd volume, the 10th phase, p5～7).More specifically, the olefin cracking catalyzer is made up of process P or alkali-earth metal modified ZSM-5 molecular sieve, for example the BOC of Beijing Chemical Research Institute catalyzer.
In concrete enforcement of the present invention, different raw materials can be mixed the back and introduce in the dehydrogenation reactor; After also different raw material can being introduced different dehydrogenation reactors and using different catalyzer and condition to carry out dehydrogenation reaction, together the product after the dehydrogenation is mixed again and handle.
In the method for the invention, described low-carbon alkene refers to that mainly carbonatoms is less than 5 alkene.
Method of the present invention has following beneficial effect:
1, uses method of the present invention, the temperature of carrying out petroleum hydrocarbon dehydrogenation and olefin reaction is significantly less than existing preparing ethylene by steam cracking and catalytic pyrolysis technology, can save big energy and high temperature resistant equipment, equipment operation maintenance, investment are lower, realize easily on engineering.
2, because the starting stage that method of the present invention adopts dehydrogenation reaction to make reaction, utilize simple gas-liquid separation that hydrogen and other logistics are separated, and in follow-up reactive system, seldom generate hydrogen and methane in the product, thereby in reaction process, reduced separating of hydrogen and low carbon number materials such as methane and purpose product low-carbon alkene, do not had simultaneously to greatly reduce isolating energy consumption with the alkane of carbon atom and separating of alkene.
3, use method of the present invention, the yield height of the purpose product of the steam cracking that the yield of purpose product low-carbon alkene is more traditional.
4, the technical process of method of the present invention is simpler than the technical process of traditional technique for producing ethylene.
Embodiment
Embodiment 1
Fresh whiteruss (C
4～C
20) through the interchanger preheating, reach 500 ℃, enter and contain in the dehydrogenation reactor that platinum is Primary Catalysts (produced by the Beijing Chemical Research Institute, the trade mark: BDH, main active component is the Pt/ aluminum oxide), reaction pressure 0.06MPa, weight space velocity is 3h during liquid
-1, catalytic dehydrogenating reaction takes place, obtain comprising hydrogen, unreacted alkane and with the mixture of reaction raw materials with the alkene of carbon number; Be introduced into the hydrogen burning reactor again, under the condition that catalyzer (produced by the Beijing Chemical Research Institute, the trade mark: BHO, main active component is the Pt/ aluminum oxide) exists, at reaction conditions be: weight hourly space velocity 3h
-1, reaction pressure 0.06MPa, water vapour and oil weight ratio 0.5, with hydrogen in the logistics and the extraneous oxygen generation catalyst combustion reaction of coming that replenishes, when consuming the hydrogen of mixture, logistics is heated to 550 ℃, obtaining forming is unreacted raw material liq paraffin, reaches and the olefin stream of raw material with carbon number; Enter olefin reactor, (produce at catalyzer by the Beijing Chemical Research Institute, the trade mark: BOC, main active component is P and alkali-earth metal modified ZSM-5 molecular sieve catalyst) effect is down, reaction pressure still maintains about 0.06MPa, the product composition is listed in the table 1, and surplus is a unreacting material, enters separation system and separates.Can select methods such as existing low temperature separation process, middle cold oil absorption, gas separation unit, extraction, catalytic distillation to separate according to the difference of downstream flow process.Unreacted raw material preferably mixes with fresh raw material as raw material after separating.
Scission reaction can not take place at 550 ℃ in same raw material, can not obtain low-carbon alkene products such as any ethene, propylene, mixed butene.
Table 1
The present invention is in the method for raw material producing light olefins with the whiteruss, and the hydrogen burning process combines with the hydro carbons catalytic process, makes whiteruss directly obtain heat, has improved heat transfer efficiency, has saved energy.Product seldom generates small molecules products such as hydrogen and methane in forming, thereby in reaction process, reduced separating of hydrogen and low carbon number materials such as methane and purpose product low-carbon alkene, do not had simultaneously to greatly reduce isolating energy consumption with the alkane of carbon atom and separating of alkene.
Claims (9)
1. a method of producing low-carbon alkene is characterized in that, described method comprises the following steps:
(1) dehydrogenation: petroleum hydrocarbon raw material is sent into dehydrogenation reactor, in the presence of dehydrogenation catalyst, dehydrogenation reaction takes place, obtain containing the hydrocarbon mixture of hydrogen and unsaturated hydro carbons;
(2) hydrogen burning: the hydrogen burning reactor is introduced in the logistics that contains hydrogen and unsaturated hydrocarbons compounds that step (1) obtains, in the presence of hydrogen burning catalyst, hydrogen in the described logistics and the outside oxygen generation combustion reactions of supplying with, the petroleum hydrocarbon material is heated to olefin catalytic transforms needed temperature, obtain the unsaturated hydro carbons mixture of moisture vapor;
(3) conversion of olefines: the unsaturated hydro carbons mixture of the moisture vapor that step (2) is obtained is introduced olefin reactor, carries out olefin reaction in the presence of the conversion of olefines catalyzer, obtains containing C
2～C
4The logistics of alkene;
(4) separate: contain C what step (3) obtained
2～C
4The logistics of alkene is introduced separation circuit and is separated, and obtains being rich in C
2The product of alkene, be rich in C
3The product of alkene and be rich in C
4The product of alkene.
2. the method for claim 1, it is characterized in that, in described step (2), the described logistics that contains hydrogen and unsaturated hydrocarbons compounds is introduced described hydrogen burning reactor with thinner, in the presence of hydrogen burning catalyst, hydrogen and the outside oxygen generation combustion reactions of supplying with;
In step (3), enter that olefin(e) centent is not higher than 50% in the logistics of olefin reactor, preferably be not higher than 35%, more preferably no higher than 20%.
3. method as claimed in claim 2 is characterized in that, in described step (2), described thinner is a water vapor.
4. the method for claim 1 is characterized in that, in described step (4), described separation circuit comprises compression, rectifying, extraction and low temperature separation process process.
5. the method for claim 1 is characterized in that, in described step (4), obtains ethylene product, propylene product, butylene product and product butadiene by separation.
6. method as claimed in claim, it is characterized in that, described dehydrogenation reactor is for adding the fixed-bed reactor or the fluidized-bed reactor of dehydrogenation catalyst, described hydrogen burning reactor is for adding the fixed-bed reactor or the fluidized-bed reactor of hydrogen burning catalyst, and described olefin reactor is for adding the fixed-bed reactor or the fluidized-bed reactor of conversion of olefines catalyzer.
7. method as claimed in claim 6, it is characterized in that, described dehydrogenation reactor is the fixed-bed reactor that add dehydrogenation catalyst, described hydrogen burning reactor is for adding the fixed-bed reactor of hydrogen burning catalyst, and described olefin reactor is to add the fixed-bed reactor of conversion of olefines catalyzer.
8. method as claimed in claim 6 is characterized in that, it is dehydrogenation catalyst or nickel catalyst that described dehydrogenation catalyst is selected from carried noble metal Pt, and described hydrogen burning catalyst is selected from carried noble metal Pt or Pd is a hydrogen burning catalyst; Described conversion of olefines catalyzer is one or more the mixture in modification or unmodified ZSM-5, ZSM-11, ZSM-23, MCM-22 and the SAPO molecular sieve catalysts.
9. the method for claim 1 is characterized in that, described petroleum hydrocarbon raw material is one or more the mixture in petroleum naphtha, diesel oil, whiteruss, solid paraffin, normal paraffin mixture, hydrogenation tail oil, tops and the reformate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910082941A CN101870632A (en) | 2009-04-27 | 2009-04-27 | Method for producing low-carbon olefin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910082941A CN101870632A (en) | 2009-04-27 | 2009-04-27 | Method for producing low-carbon olefin |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101870632A true CN101870632A (en) | 2010-10-27 |
Family
ID=42995736
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910082941A Pending CN101870632A (en) | 2009-04-27 | 2009-04-27 | Method for producing low-carbon olefin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101870632A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659076A (en) * | 2012-04-19 | 2012-09-12 | 陕西延长石油（集团）有限责任公司 | Method for co-production of various chemical products from natural gas, coal and petroleum |
| CN111040811A (en) * | 2018-10-15 | 2020-04-21 | 中国石油化工股份有限公司 | Catalytic cracking method and system for heavy oil raw material |
| CN116059988A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Paraffin hydrogenation catalyst and synthesis method and application thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4914249A (en) * | 1988-12-29 | 1990-04-03 | Uop | Dehydrogenation of dehydrogenatable hydrocarbons |
| CN101348409A (en) * | 2007-07-19 | 2009-01-21 | 中国石油化工股份有限公司 | Method for producing low carbon alkene |
-
2009
- 2009-04-27 CN CN200910082941A patent/CN101870632A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4914249A (en) * | 1988-12-29 | 1990-04-03 | Uop | Dehydrogenation of dehydrogenatable hydrocarbons |
| CN101348409A (en) * | 2007-07-19 | 2009-01-21 | 中国石油化工股份有限公司 | Method for producing low carbon alkene |
Non-Patent Citations (1)
| Title |
|---|
| 李玉敏: "《工业催化原理》", 30 November 1992, 天津大学出版社 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659076A (en) * | 2012-04-19 | 2012-09-12 | 陕西延长石油（集团）有限责任公司 | Method for co-production of various chemical products from natural gas, coal and petroleum |
| CN111040811A (en) * | 2018-10-15 | 2020-04-21 | 中国石油化工股份有限公司 | Catalytic cracking method and system for heavy oil raw material |
| CN111040811B (en) * | 2018-10-15 | 2021-10-08 | 中国石油化工股份有限公司 | Catalytic cracking method and system for heavy oil raw material |
| CN116059988A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Paraffin hydrogenation catalyst and synthesis method and application thereof |
| CN116059988B (en) * | 2021-10-29 | 2024-06-04 | 中国石油化工股份有限公司 | Paraffin hydrogenation catalyst and synthesis method and application thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101348409B (en) | Method for producing low carbon alkene | |
| CN101376823B (en) | Benzin naphtha catalytic reforming method | |
| CN104250186B (en) | A kind of preparation method of low-carbon alkene | |
| CN103121894A (en) | Combined method for producing low-carbon olefin | |
| CN101195554B (en) | Method for producing low carbon olefin hydrocarbon with C4 hydrocarbon | |
| CN103772126B (en) | Take oil refinery dry gas as the combined method of waste ethylbenzene | |
| CN103121892A (en) | Method for producing low-carbon olefin by alkane | |
| CN101863729A (en) | Method for preparing low-carbon olefin by hydrocarbon cracking | |
| CN103058814B (en) | Method for producing aromatic hydrocarbon and olefin from liquefied gas | |
| CN100457857C (en) | Method for producing olefin through catalytic cracking | |
| CN103864564B (en) | Technique for processing methanol-to-propylene by-products | |
| CN101870632A (en) | Method for producing low-carbon olefin | |
| CN102285851B (en) | Method for increasing yields of ethylene and propylene | |
| CN105189412A (en) | Process and plant for producing olefins from oxygenates | |
| CN101870631A (en) | Method for producing low-carbon olefins by using petroleum hydrocarbon | |
| CN102286292B (en) | Method for increase production of propylene and ethylene by pyrolyzing C4 raffinate | |
| CN101845320A (en) | Method for producing low-carbon olefin | |
| CN102899084B (en) | Method for co-production of pyrolysis raw material for ethylene through C4 hydrocarbon aromatization | |
| CN102285853A (en) | Method for increasing yield of propylene and ethylene by using cracked C4 as raw material | |
| CN101870633A (en) | Method for producing low-carbon olefins by using petroleum hydrocarbon | |
| CN101870630B (en) | Method for preparing low-carbon olefin by hydrocarbon catalytic pyrolysis combined with hydrogen burning technology | |
| CN108017485B (en) | Process for preparing aromatic hydrocarbon and combustible gas from methanol | |
| CN105418347B (en) | A kind of method that biological methane photoactivation anaerobic aromatization prepares aromatic hydrocarbons | |
| CN104250188B (en) | A kind of preparation method of low-carbon alkene | |
| CN111560267B (en) | Method for producing high-octane low-benzene gasoline |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20101027 |