CN111116287A - Process for the preparation of propylene and ethylene - Google Patents
Process for the preparation of propylene and ethylene Download PDFInfo
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- CN111116287A CN111116287A CN201811275245.XA CN201811275245A CN111116287A CN 111116287 A CN111116287 A CN 111116287A CN 201811275245 A CN201811275245 A CN 201811275245A CN 111116287 A CN111116287 A CN 111116287A
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- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 34
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 239000005977 Ethylene Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims description 44
- 238000002360 preparation method Methods 0.000 title claims description 4
- 150000001336 alkenes Chemical class 0.000 claims abstract description 149
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 106
- 238000005336 cracking Methods 0.000 claims abstract description 32
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 30
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 29
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 27
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 21
- 239000000463 material Substances 0.000 claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims description 29
- 239000003054 catalyst Substances 0.000 claims description 23
- 238000010992 reflux Methods 0.000 claims description 8
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 238000006471 dimerization reaction Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000003377 acid catalyst Substances 0.000 claims 1
- 239000008188 pellet Substances 0.000 claims 1
- 238000003786 synthesis reaction Methods 0.000 claims 1
- 239000002994 raw material Substances 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 3
- -1 propylene, ethylene Chemical group 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 229910052799 carbon Inorganic materials 0.000 description 11
- HQQADJVZYDDRJT-UHFFFAOYSA-N ethene;prop-1-ene Chemical group C=C.CC=C HQQADJVZYDDRJT-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 239000002808 molecular sieve Substances 0.000 description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 4
- CZXDHMZKNAOPHQ-VOTSOKGWSA-N [(5e)-10-propyltrideca-5,9-dienyl] acetate Chemical compound CCCC(CCC)=CCC\C=C\CCCCOC(C)=O CZXDHMZKNAOPHQ-VOTSOKGWSA-N 0.000 description 3
- IAQRGUVFOMOMEM-UHFFFAOYSA-N but-2-ene Chemical compound CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 3
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003085 diluting agent Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- XNMQEEKYCVKGBD-UHFFFAOYSA-N dimethylacetylene Natural products CC#CC XNMQEEKYCVKGBD-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 150000005673 monoalkenes Chemical class 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 230000000379 polymerizing effect Effects 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical class [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 238000005829 trimerization reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method for producing ethylene and propylene by using C4～C6The hydrocarbon material flow is sent to an olefin polymerization unit to obtain C8 +A first stream of olefin components, and separating C8 +All or part of the olefin components are sent to an olefin cracking unit to obtain propylene, ethylene and C4～C6Hydrocarbons, C obtained by cracking olefins in a unit4～C6The technical proposal of recycling all or part of the hydrocarbon material flow to the olefin polymerization unit and/or the olefin cracking unit has the characteristics of small circulation, low energy consumption, good economy and the like, and is particularly suitable for raw materials with lower olefin concentration.
Description
Technical Field
The invention relates to a method for preparing propylene and ethylene, in particular to a method for preparing propylene and ethylene by utilizing a catalysis method.
Background
The olefin catalytic cracking technology is a method for obtaining light molecular olefins of propylene and ethylene by utilizing various mixed C4-C6 as raw materials and catalytically cracking the olefins contained in the raw materials usually in the presence of a molecular sieve catalyst. Currently, representative olefin catalytic cracking processes mainly include: a Propylur process, an OCP process, an Omega process, an OCC process and a Superflex process. The Propylur process is developed by Germany Lurgi company, a fixed bed reaction process is adopted, steam is used as a diluting raw material, a molecular sieve catalyst is adopted, the reaction is carried out in an adiabatic way at 500 ℃ and 0-0.1 MPaG, and a reactor is in a fixed bed type and is provided with one reactor for two reactors; the ratio of the steam to the raw material is 0.5-3.0, and the service life of the catalyst reaches 15 months. The olefin conversion rate of the Propylur process reaches 85%, the once-through propylene yield is 40 mol%, and the ethylene yield is 10 mol% (relative to the total amount of olefins in the feed); the process has a set of demonstration devices in German Worringer, and no industrial devices are built at present. The OCP process is developed by cooperation of UOP and Atofina, a fixed bed reaction process is adopted, and the reaction is carried out at 500-600 ℃ and 0.1-0.4 MPaG; a reaction system with high space velocity and no diluent gas is adopted. The Omega process was developed by Asahi Kasei corporation of Japan, the reaction was carried out in a single-stage, adiabatic fixed bed, and the catalyst was regenerated by switching between the two reactors; a molecular sieve catalyst is adopted, the reaction is carried out at 530-600 ℃ and 0-0.5 MPaG, the reaction space velocity WHSV is 3-10 h < -1 >, and the olefin conversion rate of the process is more than 75%. The Asahi formation in 2006 6 months creates a set of devices for producing propylene by an Omega method in the water island. The OCC process was developed by Shanghai institute of petrochemical engineering and the reaction was carried out adiabatically in a fixed bed. A process without diluent gas is adopted, the reaction airspeed WHSV is 15-30 h < -1 >, the reaction pressure is 0-0.15 MPaG, the reaction temperature is 500-560 ℃, and the single-pass conversion rate of olefin is more than 65%. The OCC process established a 100 ton/year scale pilot plant in early 2004 at shanghai petrochemical co ltd. In 2009, an OCC industrial plant of 6 ten thousand tons/year size was built in central petrochemical limited.
The olefin polymerization technology is a method for non-selectively polymerizing C8 olefin by using mixed hydrocarbon, in particular C4 olefin in mixed C4 raw material through a catalyst. The OliHyd process is developed by China petrochemical Shanghai petrochemical research institute, the reaction is carried out in a tubular reactor, a solid phosphoric acid catalyst is adopted, the reaction is carried out at the temperature of 160-220 ℃, and the reaction airspeed WHSV is 1.5-3.0 h < -1 >. The Lanzhou petrochemical used the process and the Shanghai institute T-99 catalyst in 2004 for industrial application on carbon tetramerization plants. The light carbon four and the heavy carbon four are respectively used, and the average conversion rate of the olefin is more than 81 percent.
Disclosure of Invention
The invention aims to solve the technical problem of poor economy when the olefin cracking technology is used for treating the raw material with low olefin concentration in the prior art, and provides a novel method for producing ethylene and propylene.
Olefin cracking technology is used commercially to treat lower concentration feedstocks, such as carbon four in refineries, and in order to achieve higher overall conversion, unreacted feedstock is often recycled back to the olefin cracking unit for processing. Because the boiling points of the olefin and the alkane in the unreacted materials are relatively close (such as n-butane and 2-butene), a large amount of alkane which does not participate in the reaction returns to the reactor along with the olefin, so that the reaction system is supported too large, and the energy consumption is also greatly increased.
The industrial olefin polymerization technology is mainly used for oil refining enterprises, and as the generated product is olefin, the olefin is often blended into a gasoline pool through further hydrogenation along with the upgrading of the quality of oil products, so that the industrial olefin polymerization technology is not dominant in competition with a direct alkylation route. Under the large background that oil refining enterprises seek for chemical transformation, blending light hydrocarbon which can be utilized in chemical engineering into a gasoline pool is also a waste of resources.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: a process for the production of propylene and ethylene comprising the steps of:
(1) c is to be4～C6The hydrocarbon material flow is sent to an olefin polymerization unit to obtain C8 +A first stream of olefin components;
(2) separating (e.g. rectifying) said first stream to obtain C8 +An olefin component;
(3) c obtained in the step (2)8 +The olefin component is sent to an olefin cracking unit to obtain propylene and ethylene, and C4～C6A hydrocarbon;
(4) c obtained in the step (3)4～C6The hydrocarbon stream is wholly/partly recycled to the olefin polymerization unit and/or the olefin cracking unit.
In the above technical solution, preferably, C in the step (4)4～C6At least 10 wt% (preferably at least 30 wt%, at least 70 wt%, at least 90 wt%) of the hydrocarbon stream is recycled to the olefin folding and/or olefin cracking unit.
In the above technical solution, preferably, C in the step (4)4～C6At least 10 wt% (preferably at least 30 wt%, at least 70 wt%, at least 90 wt%) of the hydrocarbon stream is recycled to the olefin cracking unit.
In the above technical solution, preferably, C in the step (4)4～C6At least 10 wt% (preferably at least 30 wt%, at least 70 wt%, at least 90 wt%) of the hydrocarbon stream is recycled to the olefin polymerization unit.
In the above technical scheme, the first stream in the step (1) also contains rich C4～C6Hydrocarbon component of alkane, which is reacted with C in step (2)8 +And (4) separating an olefin component.
In the above technical solution, preferably, the separation is achieved in a separation unit; the separation unit comprises at least eight decarbonization towers.
In the above technical solution, it is preferable that at least the reaction of cracking the olefin into ethylene and propylene occurs in the olefin cracking unit.
In the above technical solution, it is preferable that the dimerization, trimerization and the like of the C4 to C8 olefins occur in the olefin polymerization unit, and at least the olefin dimerization reaction should be included.
In the above technical solution, preferably, the catalyst used in the olefin cracking unit comprises a molecular sieve catalyst.
In the above technical scheme, preferably, the catalyst used in the olefin cracking unit contains a ZSM-5 catalyst.
In the above technical solution, preferably, the catalyst used in the olefin polymerization unit is an acidic catalyst.
In the above technical solution, preferably, the catalyst used in the olefin polymerization unit is a solid phosphoric acid or a small silica-alumina ball catalyst.
In the above technical solution, preferably, C4～C6The hydrocarbon stream containing a component selected from C4～C6At least one olefin of the olefins.
In the above technical solution, preferably, the separation method in step (2) is one or a combination of rectification, split-flow and absorption methods; the rectification method is preferred, and the more preferred conditions for rectification are as follows: the tower pressure is 0-0.2 MPa (gauge pressure), the number of theoretical plates is 5-20, and the reflux ratio is 0.1-3.
In the technical scheme of the invention, C generated by superposition8 +The olefin component is defined as: olefin hydrocarbon material with carbon number not less than 8. C8 +Olefin component with C8+The expression olefin component is meant to be identical.
By adopting the technical scheme of the invention, C can be polymerized by an olefin polymerization method4～C6The effective raw material (olefin) in the raw material is changed into C with high conversion rate8 +Olefin component, thus and C not participating in the reaction4～C6The alkane is separated, so that the alkane is prevented from entering an alkene cracking reactor, the scale and the energy consumption of the device can be greatly reduced, and a good technical effect is achieved.
The invention is further illustrated by the following examples.
Drawings
FIG. 1 is a schematic process flow diagram of a preferred embodiment of the present invention.
I is an olefin polymerization unit;
II is a separation unit (preferably comprising eight decarbonation columns);
III is an olefin cracking unit;
1 is C4～C6A hydrocarbon stream feed;
2 is a stream comprising propylene and ethylene produced by an olefin cracking unit;
3 is C obtained by separating olefin polymerization product8 +An olefin component;
4 is C produced in an olefin cracking unit4～C6Hydrocarbons (recycled back to the olefin polymerization unit);
5 is C produced in an olefin cracking unit4～C6Hydrocarbons (recycled back to the olefin cracking unit);
6 is the product of an olefin polymerization unit;
FIG. 2 is a schematic process flow diagram of a conventional process.
I is an olefin cracking unit;
1 is hydrocarbon material flow raw material;
2 is an ethylene propylene containing stream produced by an olefin cracking unit;
8 is unreacted materials (discharge battery limit zone);
9 is unreacted materials (recycled to the olefin cracking unit);
10 is an unreacted hydrocarbon stream feed;
Detailed Description
The following detailed description of the embodiments of the present invention is provided, but it should be noted that the scope of the present invention is not limited by the embodiments, but is defined by the appended claims.
All publications, patent applications, patents, and other references mentioned in this specification are herein incorporated by reference in their entirety. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In case of conflict, the present specification, including definitions, will control.
When the specification concludes with claims with the heading "known to those skilled in the art", "prior art", or the like, to derive materials, substances, methods, procedures, devices, or components, etc., it is intended that the subject matter derived from the heading encompass those conventionally used in the art at the time of filing this application, but also include those that are not currently in use, but would become known in the art to be suitable for a similar purpose.
In the context of the present invention, the term "C4 olefin" or "C4An olefin "refers to a mono-olefin having four carbon atoms. For example, as C4 olefins, various isomers of butenes such as 1-n-butene, 2-n-butene, and isobutene are contemplated.
In the context of the present invention, the terms "C4-C6 olefin" and "C4-C6The olefins "identical" refer to C4 olefins, C5 olefins, and C6 olefins.
Unless otherwise expressly indicated, all percentages, parts, ratios, etc. mentioned in this specification are by weight unless otherwise not in accordance with the conventional knowledge of those skilled in the art.
In the context of this specification, any two or more embodiments of the invention may be combined in any combination, and the resulting solution is part of the original disclosure of this specification, and is within the scope of the invention.
[ example 1 ]
The flow shown in fig. 1 is adopted:
Stream 6 (flow rate 1000kg/h, C) from I8 +An olefin content of 455kg/h) was fed into II, which was operated under the following conditions: 0.1MPa (gauge pressure), reflux ratio 0.5, 10 theoretical plates, stream 3 obtained by separating II (the flow rate is 450kg/h, wherein C8 +Olefin content greater than 95%) is fed to III.
All the C4-C6 hydrocarbons obtained in III are recycled to III. The flow rate of stream 5 was 264 kg/h.
The total inventory entering the unit III was 714kg/h for stream 5+ stream 3.
III gives a stream 2 containing 86kg/h of ethylene and 257g/h of propylene, giving an ethylene-propylene yield of 68.6% based on the available starting material (olefins) in stream 1.
[ example 2 ]
The flow shown in fig. 1 is adopted:
Stream 6 (flow rate 1000kg/h, C) from I8 +An olefin content of 455kg/h) was fed into II, which was operated under the following conditions: 0.1MPa (gauge pressure), reflux ratio 0.5, 10 theoretical plates, stream 3 obtained by separating II (the flow rate is 474kg/h, wherein C8 +Olefin content greater than 95%) is fed to III.
90% of all C4-C6 hydrocarbons obtained in III are recycled back to III, and the remaining 10% are returned to I. The flow rate of stream 5 was 236 kg/h.
The total charge to the unit III was 710kg/h for stream 5+ stream 3.
III gave a stream 2 containing 85 kg/h ethylene and 255g/h propylene with an ethylene-propylene yield of 68.0% based on the active feed (olefin) in stream 1.
[ example 3 ]
The flow shown in fig. 1 is adopted:
Stream 6 (flow rate 1000kg/h, C) from I8 +An olefin content of 455kg/h) was fed into II, which was operated under the following conditions: 0.1MPa (gauge pressure), reflux ratio 0.5, 10 theoretical plates, stream 3 obtained by separating II (the flow rate is 520kg/h, wherein C8 +Olefin content greater than 95%) is fed to III.
70% of all C4-C6 hydrocarbons obtained in III are recycled back to III, and the remaining 30% are returned to I. The flow rate of stream 5 was 182 kg/h.
The total charge to the unit III was 702kg/h for stream 5+ stream 3.
[ example 4 ]
The flow shown in fig. 1 is adopted:
Stream 6 (flow rate 1000kg/h, C) from I8 +An olefin content of 455kg/h) was fed into II, which was operated under the following conditions: 0.1MPa (gauge pressure), reflux ratio 0.5, 10 theoretical plates, stream 3 obtained by separating II (the flow rate is 610kg/h, wherein C8 +Olefin content greater than 95%) is fed to III.
30% of all C4-C6 hydrocarbons obtained in III are recycled back to III, and the remaining 70% are returned to I. The flow rate of stream 5 was 76 kg/h.
The total charge to the unit III was 686kg/h for stream 5+ stream 3.
[ example 5 ]
The flow shown in fig. 1 is adopted:
Stream 6 (flow rate 1000kg/h, C) from I8 +An olefin content of 455kg/h) was fed into II, which was operated under the following conditions: 0.1MPa (gauge pressure), reflux ratio 0.5, 10 theoretical plates, stream 3 obtained by separating II (the flow rate is 653kg/h, wherein C8 +Olefin content greater than 95%) is fed to III.
10% of all C4-C6 hydrocarbons obtained in III are recycled back to III, and the remaining 70% are returned to I. The flow rate of stream 5 was 25 kg/h.
The total inventory entering unit III was 678kg/h for stream 5+ stream 3.
[ example 6 ]
The flow shown in fig. 1 is adopted:
Stream 6 (flow rate 1000kg/h, C) from I8 +An olefin content of 455kg/h) was fed into II, which was operated under the following conditions: 0.1MPa (gauge pressure), reflux ratio 0.5, 10 theoretical plates, stream 3 obtained by separating II (the flow rate is 675kg/h, wherein C8 +Olefin content greater than 95%) is fed to III.
All of the C4-C6 hydrocarbons obtained in III were returned to I. The flow rate of stream 5 was 0 kg/h.
The total charge to the unit III was 675kg/h, stream 5+ stream 3.
Comparative example 1
The flow shown in fig. 2 is adopted:
82% of the stream 10 resulting from I (flow rate 3253kg/h, C4-C8 olefin content 293kg/h) was returned to I.
The reaction materials entering the reactor I are a material flow 1 and a material flow 9, wherein the flow rate of the material flow 1 is 1000kg/h, the flow rate of the material flow 9 is 2667kg/h, and the total amount is 3667 kg/h.
Comparative example 2
The flow shown in fig. 2 is adopted:
50% of the stream 10 resulting from I (with a flow rate of 1275kg/h and a C4-C8 olefin content of 276kg/h) was returned to I.
The reaction mass entering into I was stream 1 and stream 9, wherein the flow of stream 1 was 1000kg/h, the flow of stream 9 was 638kg/h, and the total amount was 1638 kg/h.
A list of specific embodiments is shown in table 1.
TABLE 1
Claims (10)
1. A process for the production of propylene and ethylene comprising the steps of:
(1) c is to be4～C6The hydrocarbon material flow is sent to an olefin polymerization unit to obtain C8 +A first stream of olefin components;
(2) separating (e.g. rectifying) said first stream to obtain C8 +An olefin component;
(3) c obtained in the step (2)8 +The olefin component is sent to an olefin cracking unit to obtain propylene and ethylene, and C4～C6A hydrocarbon;
(4) c obtained in the step (3)4～C6The hydrocarbon stream is wholly/partly recycled to the olefin polymerization unit and/or the olefin cracking unit.
2. The process for producing propylene and ethylene according to claim 1, wherein C in the step (4)4～C6At least 10 wt% (preferably at least 30 wt%, at least 70 wt%, at least 90 wt%) of the hydrocarbon stream is recycled to the olefin stackA synthesis and/or olefin cracking unit.
3. The process for producing propylene and ethylene according to claim 2, wherein C in the step (4)4～C6At least 10 wt% (preferably at least 30 wt%, at least 70 wt%, at least 90 wt%) of the hydrocarbon stream is recycled to the olefin cracking unit.
4. The process for producing propylene and ethylene according to claim 1, wherein at least the reaction of olefin cracking into ethylene and propylene occurs in the olefin cracking unit.
5. Process for the preparation of propylene and ethylene according to claim 1, characterized in that at least olefin dimerization occurs in the olefin polymerization unit.
6. Process for the preparation of propylene and ethylene according to claim 1, characterized in that the first stream in step (1) contains a C rich fraction4～C6Hydrocarbon component of alkane, which is reacted with C in step (2)8 +And (4) separating an olefin component.
7. The process for producing propylene and ethylene according to claim 1, wherein the catalyst used in the olefin cracking unit comprises a molecular sieve-type catalyst; preferably the catalyst comprises a ZSM-5 type catalyst.
8. The process for the production of propylene and ethylene according to claim 1, characterized in that the catalyst used in the olefin polymerization unit is an acid catalyst; preferably the catalyst is a solid phosphoric acid or a silica-alumina pellet catalyst.
9. The process for preparing propylene and ethylene according to claim 1, characterized in that C4～C6The hydrocarbon stream containing a component selected from C4～C6At least one olefin of the olefins.
10. The process for preparing propylene and ethylene according to claim 1, wherein the separation method in step (2) is selected from one or a combination of rectification, split-flow and absorption methods; the rectification method is preferred, and the more preferred conditions for rectification are as follows: the tower pressure is 0-0.2 MPa (gauge pressure), the number of theoretical plates is 5-20, and the reflux ratio is 0.1-3.
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| CN201811275245.XA CN111116287A (en) | 2018-10-30 | 2018-10-30 | Process for the preparation of propylene and ethylene |
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| CN201811275245.XA CN111116287A (en) | 2018-10-30 | 2018-10-30 | Process for the preparation of propylene and ethylene |
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|---|---|---|---|---|
| CN1642887A (en) * | 2002-03-15 | 2005-07-20 | 法国石油公司 | Multi-step method of converting a charge containing olefins with four, five or more carbon atoms in order to produce propylene |
| US20080287717A1 (en) * | 2006-07-19 | 2008-11-20 | Kuechler Keith H | Feedstock preparation of olefins for oligomerization to produce fuels |
| CN102531824A (en) * | 2011-12-29 | 2012-07-04 | 北京惠尔三吉绿色化学科技有限公司 | Process method for preparing propylene and ethylene from liquid gas including butylene |
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2018
- 2018-10-30 CN CN201811275245.XA patent/CN111116287A/en active Pending
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|---|---|---|---|---|
| CN1642887A (en) * | 2002-03-15 | 2005-07-20 | 法国石油公司 | Multi-step method of converting a charge containing olefins with four, five or more carbon atoms in order to produce propylene |
| US20080287717A1 (en) * | 2006-07-19 | 2008-11-20 | Kuechler Keith H | Feedstock preparation of olefins for oligomerization to produce fuels |
| CN102531824A (en) * | 2011-12-29 | 2012-07-04 | 北京惠尔三吉绿色化学科技有限公司 | Process method for preparing propylene and ethylene from liquid gas including butylene |
Non-Patent Citations (1)
| Title |
|---|
| 张祥剑等: "混合碳四烯烃叠合利用工艺技术研究", 《齐鲁石油化工》 * |
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Application publication date: 20200508 |