CN112707780A - Method for producing ethylene and propylene from raw materials with four or more carbon atoms - Google Patents

Method for producing ethylene and propylene from raw materials with four or more carbon atoms Download PDF

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CN112707780A
CN112707780A CN201911019049.0A CN201911019049A CN112707780A CN 112707780 A CN112707780 A CN 112707780A CN 201911019049 A CN201911019049 A CN 201911019049A CN 112707780 A CN112707780 A CN 112707780A
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carbon
stream
raw material
carbons
reaction
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金鑫
杨卫胜
卢和泮
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

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  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a method for producing ethylene and propylene by using four or more carbon raw materials, which comprises the following steps: (1) providing a carbon four raw material and a carbon five raw material and above; (2) carrying out olefin catalytic cracking treatment on the carbon four raw material to obtain a reaction product; (3) separating the reaction product to obtain a material flow with the carbon number of three or less and a material flow with the carbon number of four or more; (4) separating the raw material with five or more carbons and the material flow with four or more carbons to obtain light component material flow and crude gasoline; (5) recycling part of the light component stream to the step (2) for olefin catalytic cracking treatment. The method separates the components which are easy to cause the rapid coking of the catalyst in the raw materials of five carbon and above, and controls the content of the components which are easy to coke in the circulating material, thereby controlling the concentration of the components which are easy to coke in the material entering the reactor, achieving the purposes of slowing down the coking of the catalyst, prolonging the regeneration period and prolonging the service life of the catalyst, and obtaining better technical effects.

Description

Method for producing ethylene and propylene from raw materials with four or more carbon atoms
Technical Field
The invention relates to a method for producing ethylene and propylene by using raw materials with four or more carbon atoms.
Background
The usage of ethylene and propylene in China has been expanding in recent years. In order to meet the market demand, a large number of methanol-to-olefin devices are newly built, and simultaneously, a plurality of million-ton-level oil refining and chemical engineering integrated projects are also approved, built or put into production. These apparatuses produce ethylene and propylene through different process routes while producing a large amount of hydrocarbons of carbon four and carbon five and more. The four-carbon hydrocarbon is utilized in many ways, and the industrialized technology comprises olefin catalytic cracking, production of gasoline additive methyl tert-butyl ether, production of alkylate oil by isobutene superposition hydrogenation and the like. Methyl tert-butyl ether generation devices are commonly arranged in various large refineries, and the methyl tert-butyl ether is produced as a gasoline additive by utilizing isobutene in the byproduct C4. However, with the wide spread of ethanol gasoline and the policy of prohibiting the artificial addition of methyl tert-butyl ether to gasoline pools, a large number of devices for utilizing the byproduct carbon four through the methyl tert-butyl ether pathway have to find new utilization approaches. It is against this background that olefin catalytic cracking technology has met with tremendous market opportunities.
The olefin catalytic cracking is a technology for producing ethylene and propylene by catalytic cracking reaction of C4-C6 olefin. The raw materials of the existing industrialized olefin catalytic cracking device are MTO by-product carbon four-carbon five-hydrocarbon, and do not contain or only contain trace amount of heavier hydrocarbon, and the circulating material is also carbon four-carbon five-hydrocarbon. For example, in the patent technology disclosed in CN1927784, the cracked product is separated in a rectifying tower, and the four-carbon and five-carbon components are separated from the top of a rectifying tower and recycled as the catalytic cracking raw material in 22-76 wt%. Patent CN101092323 discloses a method for preparing light olefins by catalytic cracking using a mixture containing C4-C8 carbon-containing olefins as a raw material. The method does not specify the content of heavy components in the raw materials, and the circulating material is C4 component separated from the top of the debutanizer.
However, heavy components in the cracking raw material, especially aromatic hydrocarbons such as benzene, toluene, xylene, etc., are easily coked on the surface of the catalyst, resulting in gradual deactivation of the catalyst. In order to restore the activity of the catalyst, the catalyst needs to be regenerated by burning. In order to prolong the switching period of the reaction regeneration of the catalyst, patent CN107915564 discloses a method for producing ethylene and propylene by using carbon four-carbon octaolefins containing a coking inhibitor as raw materials. The coking inhibitor is selected from sulfur compounds, preferably sulfur organic compounds. By adding the coking inhibitor into the raw materials, the activity of the catalyst is improved to a certain extent after 96 hours, the reaction coking amount is reduced, the regeneration period of the catalyst is prolonged, and the selectivity of the reaction to ethylene and propylene is improved. However, the sulfur-containing coking inhibitor is added into the raw material, and sulfur is unavoidably converted into sulfur-containing impurities such as hydrogen sulfide after passing through a high-temperature cracking reactor and enters the product to affect the product quality.
For cracking raw materials with high heavy component content, the problems that the olefin catalytic cracking catalyst is easy to coke, the regeneration period is short or the quality of products is influenced by adding a coking inhibitor exist in the prior art are solved in a targeted manner.
Disclosure of Invention
The invention aims to solve the technical problems of easy coking and short regeneration period of a catalyst in the production process of low-carbon olefin in the prior art, and provides a novel method for producing ethylene and propylene by using hydrocarbons with four or more carbon atoms. The method has the advantages of no addition of coking inhibitor, slow down catalyst coking, and prolonged regeneration period and catalyst life.
In order to achieve the aim of the invention, the invention provides a method for producing ethylene and propylene by using four or more carbon raw materials, which comprises the following steps:
(1) providing a carbon four raw material and a carbon five raw material and above;
(2) carrying out olefin catalytic cracking treatment on the carbon four raw material to obtain a reaction product;
(3) separating the reaction product to obtain a material flow with the carbon number of three or less and a material flow with the carbon number of four or more;
(4) separating the raw material with five or more carbons and the material flow with four or more carbons to obtain light component material flow and crude gasoline;
(5) recycling part of the light component stream to the step (2) for olefin catalytic cracking treatment.
According to a preferred embodiment of the present invention, the raw material for carbon four is a raw material for carbon four that is gasified by a raw material evaporator. Including n-butane, isobutane, butene-1, isobutene, trans-and cis-butene-2, and the like.
According to some embodiments of the invention, the carbon five and above feedstock comprises at least one of benzene, toluene, xylene, and carbon seven and above components; preferably at least one of benzene, toluene and xylene.
According to a preferred embodiment of the present invention, the olefin catalytic cracking treatment comprises: and heating the raw materials, heating to the reaction temperature, and then entering a reactor to perform an olefin catalytic cracking reaction.
According to a preferred embodiment of the invention, the reaction temperature of the cracking reaction is 500-600 ℃; the reaction pressure is 0.01-0.1 MPaG; the reaction space velocity is 10-30 h-1。
According to a preferred embodiment of the present invention, the olefin catalytic cracking treatment uses a catalyst comprising SiO in terms of mole ratio of Si to Al2/Al2O3100-2000 of ZSM molecular sieve catalyst.
According to a preferred embodiment of the present invention, the feedstock is sent to an olefin catalytic cracking reaction unit comprising a heat exchanger, a heating furnace and a reactor. The raw materials are heated by a heat exchanger and a heating furnace, and enter a reactor after being heated to the reaction temperature, so that the catalytic cracking reaction of olefin is carried out.
According to a preferred embodiment of the invention, the reaction product is sent to the depropanizer after being pressurized to a pressure above 1.8MPaG by a compressor.
According to some embodiments of the present invention, in the step (3), the reaction product is sent to a depropanizer for treatment, a stream with three carbons or less is obtained at the top of the depropanizer, and a stream with four carbons or more is obtained at the bottom of the depropanizer.
According to a preferred embodiment of the present invention, ethylene propylene can be obtained by further separating the C.sub.III and the following streams. The ethylene and propylene content of the carbon three and below streams is more than 80 wt%, generally about 86 wt%.
According to some embodiments of the invention, in the step (4), the carbon five or more raw materials and the carbon four or more product streams obtained in the step (3) are sent to a circulating material separation tower for treatment, a light component material stream is obtained at the top of the tower, and the crude gasoline is obtained at the bottom of the tower.
According to a preferred embodiment of the invention, the naphtha comprises six carbon and above components.
According to a preferred embodiment of the present invention, the total content of benzene, toluene and xylene in the lights stream is not more than 0.1%, preferably not more than 0.05%, more preferably not more than 0.02%, based on 100% of the total weight of the lights stream.
According to some embodiments of the invention, the lights stream is divided into a recycle stream and an effluent stream, wherein the recycle stream is recycled to step (2) for olefin catalytic cracking treatment; the proportion of the recycle stream is above 80%.
According to a preferred embodiment of the present invention, the total content of benzene, toluene and xylene in the recycle stream is not more than 0.1%, preferably, the total content of benzene, toluene and xylene is not more than 0.05%, more preferably, the total content of benzene, toluene and xylene is not more than 0.02%, based on 100% by weight of the total recycle stream.
According to some embodiments of the invention, the recycle separation column is a depentanizer and is operated at a pressure of 0.25 to 0.45 MPaG.
According to some embodiments of the invention, the recycle separation column is a dehexanizer column operating at a pressure of 0.20 to 0.35 MPaG.
According to the preferred embodiment of the invention, the raw materials with five carbon atoms and above are fed into a circulating material separation tower, a light component stream is separated from the top of the tower, and is divided into a circulating stream and an effluent stream, and the crude gasoline is separated from the bottom of the tower. By controlling the operation conditions of the circulating material separation tower, the components which are easy to cause coking of the cracking catalyst in the raw materials with five or more carbon atoms leave the system along with the crude gasoline from the tower kettle, and the components are prevented from entering a reactor along with the circulating material flow, so that the rapid coking of the catalyst is avoided. These key heavy components include benzene, toluene, xylene, etc. which have relatively high molecular weights and are not easily cracked. The concentration of the key heavy component in the circulating material flow is controlled, so that the concentration of the key heavy component entering the reactor is controlled, the regeneration period of the catalyst is prolonged, and the minimum requirement of continuous switching of reaction regeneration is met or exceeded, so that the device meets the condition of continuous operation. For example, if the regeneration time for a unit catalyst is 72 hours, the time for the cracking catalyst to coke and deactivate, leading to a decrease in catalyst performance below the threshold value, must be greater than 72 hours, or continuous switch regeneration under conditions that meet the performance requirements of the catalyst cannot be performed.
According to the preferred embodiment of the invention, the raw material of carbon four is gasified by the raw material evaporator and then is merged with the circulating material containing key components with low content of coking suitability, the mixture enters the cracking reactor after passing through the feeding and discharging heat exchanger and the heating furnace, and the reaction product is pressurized by the compressor and then is sent to the depropanizing tower. In order to avoid the use of high-grade, low-temperature refrigerants, the compressor outlet pressure is preferably above 1.80MPaG, and under these conditions, chilled water or propylene refrigerants may be used. Separating out main product containing ethylene and propylene from the top of depropanizing tower, separating out hydrocarbon with carbon number of four or more from tower bottom, and feeding into circulating material separating tower. The recycle material separation column may be either a depentanizer or a dehexanizer depending on whether or not the carbon hexaolefins are recycled. In general, higher yields of ethylene and propylene can be obtained with the recycle of the hexaolefin, but the higher activity of the hexaolefin makes coking of the catalyst surface more likely, and therefore requires particular careful control of the levels of key components in the recycle.
By adopting the method, the components which are easy to cause rapid coking of the catalyst in the raw materials of five carbon and above are separated in the circulating material separation tower, and the content of key components which are easy to coke in the circulating material is effectively controlled, so that the concentration of the key components in the material entering the reactor is controlled, the purposes of slowing down the coking of the catalyst, prolonging the regeneration period and prolonging the service life of the catalyst are achieved, and better technical effects are obtained.
Drawings
FIG. 1 is a schematic flow diagram according to some embodiments of the inventions.
Wherein, B is a charging and discharging heat exchanger, C is a heating furnace, D is a reactor, E is a compressor, F is a depropanizing tower, and G is a circulating material separation tower. Stream 1 is a carbon four feedstock, stream 2 is a carbon five and above feedstock, stream 3 is depropanizer bottoms, stream 4 is a recycle stream, stream 5 is a carbon three and below stream, stream 6 is an effluent stream, and stream 7 is a naphtha.
Detailed Description
The present invention is further illustrated by the following examples, which are not to be construed as limiting the invention in any way.
FIG. 1 shows a flow chart of one embodiment of the present invention. The carbon four raw material 1 gasified by the raw material evaporator is mixed with a circulating material flow 4, then enters a feeding and discharging heat exchanger B and a heating furnace C, the mixture is heated to the reaction temperature and then enters a reactor D to generate olefin catalytic cracking reaction, the reaction product is subjected to waste heat recovery by the feeding and discharging heat exchanger, then enters a compressor E for pressurization and then enters a depropanizing tower F, a material flow 5 with the carbon three or less is obtained by separating from the top of the tower, a material 3 at the bottom of the tower is converged with a material 2 with the carbon five or more, the material flow enters a circulating material separation tower G, a gas phase component at the top of the tower is used as the circulating material flow 4, a liquid phase at the top of the tower is extracted as an.
[ example 1 ]
Providing a carbon four raw material with the mass flow rate of 5 tons/hour and a carbon five raw material with the mass flow rate of 10 tons/hour and above, wherein the content of butylene in the carbon four raw material is 80 percent (calculated by mass fraction, the same below), the content of pentane in the carbon five raw material is 7 percent, pentene is 62 percent, carbon hexaalkane is 4 percent, carbon hexaolefin is 15 percent, the total content of benzene, toluene and xylene (BTX) is 0.58 percent, and the balance is carbon seven and above. The scheme shown in FIG. 1 was followed, in which the recycle separation column was a depentanizer operated at a pressure of 0.30MPaG and the overhead vapor phase recycle stream had a BTX concentration of 0.0003%. The BTX concentration in the reaction feed was 0.0002%. The total yield of ethylene and propylene in the plant was 6.6 t h. The time for the catalyst conversion to decrease by 10 percentage points relative to the initial activity was 168 hours, and the catalyst regeneration time was 72 hours.
[ example 2 ]
The carbon four raw material and the carbon five raw material and above were supplied at the same flow rate and composition as in example 1. The process shown in FIG. 1 is followed, except that a dehexanizer is used as the recycle material separation column, i.e., the recycle material is hydrocarbons of carbon four, carbon five and carbon six. The operating pressure of the dehexanizer was 0.25MPaG and the BTX concentration of the overhead gas phase recycle was 0.0073%. The BTX concentration in the reaction feed was 0.0064%. The total yield of ethylene and propylene in the plant was 7.1 t h. The time for the catalyst conversion to decrease by 10 percentage points relative to the initial activity was 147 hours, and the catalyst regeneration time was 72 hours.
[ example 3 ]
A four-carbon feedstock having the same flow rate and composition as in example 1, and a five-carbon feedstock and above having a mass flow rate of 10 tons/hour, wherein the total content of pentane 5%, pentene 56%, carbon hexaalkane 6%, carbon hexaalkene 21%, benzene, toluene, xylene (BTX) is 1.2%, and the balance is carbon seven and above, were provided. The process shown in FIG. 1 is followed, except that a dehexanizer is used as the recycle material separation column, i.e., the recycle material is hydrocarbons of carbon four, carbon five and carbon six. The operating pressure of the dehexanizer was 0.30MPaG and the BTX concentration of the gas phase recycle at the top of the column was 0.0114%. The BTX concentration in the reaction feed was 0.0099%. The total yield of ethylene and propylene in the plant was 6.9 t h. The time for the catalyst conversion to decrease by 10 percentage points relative to the initial activity was 109 hours, and the catalyst regeneration time was 72 hours.
[ example 4 ]
Providing a carbon four raw material and a carbon five raw material with the same flow and composition as those of the embodiment 3, and adopting the process flow same as that of the embodiment 3, wherein the difference is that the operation condition of the dehexanizer is changed, for example, the conventional rectifying tower adjusting means such as increasing the extraction at the tower top or reducing the reflux quantity is adopted, and the BTX concentration of the gas phase circulating material at the tower top is controlled to be 0.0450%. The BTX concentration in the reaction feed was 0.0394%. The total yield of ethylene and propylene in the plant was 7.1 t h. The time for the catalyst conversion to decrease by 10 percentage points relative to the initial activity was 94 hours, and the catalyst regeneration time was 72 hours.
[ example 5 ]
The method comprises the steps of providing a carbon four raw material and a carbon five raw material with the same flow and composition as those of the raw material in the embodiment 3, and adopting the same process flow as the embodiment 3, wherein the difference is that the operation condition of the dehexanizer is changed, for example, the conventional rectifying tower adjusting means such as increasing the extraction at the tower top or reducing the reflux quantity is adopted, and the BTX concentration of the gas phase circulating material at the tower top is controlled to be 0.08%. The BTX concentration in the reaction feed was 0.0701%. The total yield of ethylene and propylene in the plant was 7.1 t h. The time for the catalyst conversion rate to decrease by 10 percentage points relative to the initial activity is 70 hours, and the catalyst regeneration time is 72 hours.
[ COMPARATIVE EXAMPLE 1 ]
The carbon four raw material and the carbon five raw material and above were supplied at the same flow rate and composition as in example 1. The difference is that the raw materials with five carbon atoms and above do not pass through a circulating material separation tower, are directly merged with the raw materials with four carbon atoms and then are sent into a device boundary area, and then are merged with the circulating materials and sent into a feeding and discharging heat exchanger according to the flow shown in the figure 1. The operating pressure of the depentanizer was 0.35MPaG, and the BTX concentration of the overhead gas-phase recycle was 0.0002%. The BTX concentration in the reaction feed was 0.14%. The time for the catalyst conversion rate to decrease by 10 percentage points relative to the initial activity is 68 hours, the catalyst regeneration time is 84 hours, and continuous reaction regeneration switching cannot be realized.
Any numerical value mentioned in this specification, if there is only a two unit interval between any lowest value and any highest value, includes all values from the lowest value to the highest value incremented by one unit at a time. For example, if it is stated that the amount of a component, or a value of a process variable such as temperature, pressure, time, etc., is 50 to 90, it is meant in this specification that values of 51 to 89, 52 to 88 … …, and 69 to 71, and 70 to 71, etc., are specifically enumerated. For non-integer values, units of 0.1, 0.01, 0.001, or 0.0001 may be considered as appropriate. These are only some specifically named examples. In a similar manner, all possible combinations of numerical values between the lowest value and the highest value enumerated are to be considered to be disclosed in this application.
It should be noted that the above-mentioned embodiments are only for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described with reference to exemplary embodiments, but the words which have been used herein are words of description and illustration, rather than words of limitation. The invention can be modified, as prescribed, within the scope of the claims and without departing from the scope and spirit of the invention. Although the invention has been described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, but rather extends to all other methods and applications having the same functionality.

Claims (10)

1. A method for producing ethylene and propylene by using four or more carbon raw materials comprises the following steps:
(1) providing a carbon four raw material and a carbon five raw material and above;
(2) carrying out olefin catalytic cracking treatment on the carbon four raw material to obtain a reaction product;
(3) separating the reaction product to obtain a material flow with the carbon number of three or less and a material flow with the carbon number of four or more;
(4) separating the raw material with five or more carbons and the material flow with four or more carbons to obtain light component material flow and crude gasoline;
(5) recycling part of the light component stream to the step (2) for olefin catalytic cracking treatment.
2. The method of claim 1, wherein the carbon five and above feedstock comprises at least one of benzene, toluene, xylene, and carbon seven and above components; preferably at least one of benzene, toluene and xylene.
3. The method according to claim 1 or 2, wherein the olefin catalytic cracking treatment comprises: and heating the raw materials, heating to the reaction temperature, and then entering a reactor to perform an olefin catalytic cracking reaction.
4. The method according to any one of claims 1 to 3, wherein the reaction temperature of the cracking reaction is 500 to 600 ℃; the reaction pressure is 0.01-0.1 MPaG; the reaction space velocity is 10-30 h-1。
5. The method according to any one of claims 1 to 4, wherein the reaction product in step (3) is sent to a depropanizer for treatment, a stream with three carbons and below is obtained at the top of the depropanizer, and a stream with four carbons and above is obtained at the bottom of the depropanizer.
6. The method of any one of claims 1 to 5, wherein in step (4), the feed containing five or more carbons and the product containing four or more carbons obtained in step (3) are sent to a recycle material separation tower for treatment, a light component stream is obtained at the top of the tower, and the naphtha is obtained at the bottom of the tower.
7. The process according to any one of claims 1 to 6, wherein the light fraction stream is divided into a recycle stream and an effluent stream, and wherein the recycle stream is recycled to step (2) for catalytic cracking of the olefin.
8. The process according to any one of claims 1 to 7, characterized in that the total content of benzene, toluene and xylene in the recycle stream is not more than 0.1%, preferably not more than 0.05%, more preferably not more than 0.02%, based on 100% by total weight of the recycle stream.
9. The process of any one of claims 1 to 8, wherein the recycle separation column is a depentanizer and is operated at a pressure of from 0.25 to 0.45 MPaG.
10. The process of any one of claims 1 to 9, wherein the recycle separation column is a dehexanizer column operating at a pressure of 0.20 to 0.35 MPaG.
CN201911019049.0A 2019-10-24 2019-10-24 Method for producing ethylene and propylene from raw materials with four or more carbon atoms Pending CN112707780A (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050150817A1 (en) * 2004-01-14 2005-07-14 Kellogg Brown And Root, Inc. Integrated catalytic cracking and steam pyrolysis process for olefins
CN101205162A (en) * 2006-12-21 2008-06-25 中国石油化工股份有限公司 Combined technique for preparing olefins by using refinery C4
CN102285852A (en) * 2010-06-18 2011-12-21 中国石油化工股份有限公司 Method for increasing yields of ethylene and propylene by using refinery C4
CN103936542A (en) * 2013-01-23 2014-07-23 中国石油化工集团公司 Alkene catalysis cracking system and method for improving alkene total conversion rate
CN105085145A (en) * 2014-05-14 2015-11-25 中国石油天然气股份有限公司 Process for producing ethylene and propylene by mixing C five-carbon hexaalkane and C four
CN105367366A (en) * 2014-08-27 2016-03-02 中国石油化工股份有限公司 Method for producing ethylene and propylene by means of mixed C4

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050150817A1 (en) * 2004-01-14 2005-07-14 Kellogg Brown And Root, Inc. Integrated catalytic cracking and steam pyrolysis process for olefins
CN101205162A (en) * 2006-12-21 2008-06-25 中国石油化工股份有限公司 Combined technique for preparing olefins by using refinery C4
CN102285852A (en) * 2010-06-18 2011-12-21 中国石油化工股份有限公司 Method for increasing yields of ethylene and propylene by using refinery C4
CN103936542A (en) * 2013-01-23 2014-07-23 中国石油化工集团公司 Alkene catalysis cracking system and method for improving alkene total conversion rate
CN105085145A (en) * 2014-05-14 2015-11-25 中国石油天然气股份有限公司 Process for producing ethylene and propylene by mixing C five-carbon hexaalkane and C four
CN105367366A (en) * 2014-08-27 2016-03-02 中国石油化工股份有限公司 Method for producing ethylene and propylene by means of mixed C4

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