CN207468520U - Produce the device of ethylene and propylene - Google Patents
Produce the device of ethylene and propylene Download PDFInfo
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- CN207468520U CN207468520U CN201721126382.8U CN201721126382U CN207468520U CN 207468520 U CN207468520 U CN 207468520U CN 201721126382 U CN201721126382 U CN 201721126382U CN 207468520 U CN207468520 U CN 207468520U
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- olefin
- ethylene
- propylene
- disproportionation
- alkene
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Abstract
Technical problem to be solved in the utility model is the problem of E/P in the prior art is smaller than adjustable amplitude, not strong to the adaptability of ethylene and propylene price fluctuation, yield of ethene is low, and E/P is smaller than adjustable amplitude, yield of ethene is low in particularly existing MTO technologies, MTO+OCC technologies.Provide the device of the production ethylene being made of olefin cracking reaction member A, olefin cracking pre-separation unit B, olefin dismutation reaction unit C, olefin(e) disproportionation pre-separation cells D and propylene, have many advantages, such as E/P than adjustable amplitude greatly, to ethylene and the adaptable of propylene price fluctuation, yield of ethene it is high, especially suitable for ethylene and propylene price difference at+500 yuan/ton.
Description
Technical field
The utility model is related to a kind of devices for producing ethylene and propylene, and in particular to a kind of device using catalysis produces
The device of ethylene and propylene.
Background technology
Triolefin technique (The Triolefin Process) is：Propylene disproportionation produces the ethylene and butene-2 of high-purity；
With the back reaction of the reaction, ethylene and butene-2 reaction generation propylene.Propylene disproportionation technology did not had industry should after 1970
Report.In recent years, being continuously increased with global propylene demand cannot have been expired using the production of propylene amount of conventional method
The demand of sufficient propylene, therefore start to industrialize using the technology of the back reaction production propylene of triolefin technique.Since the end of the year 1985,
Channelveiw of the Lyondell companies in U.S. Texas states has run a set of production of propylene device for producing 136,000 ton per year,
The technique is exactly using the cross disproportionation of ethylene and butene-2 production propylene.At home, Lummus in 2002 to Shanghai match section
The OCU technologies based on reverse triolefin technique have been transferred the possession of, later due to the great development of coal chemical industry, the C4 of many MTO devices by-products, all
With this skill upgrading added value.
Olefins by catalytic cracking technology be by the use of various mixing C4-C6 as raw material, usually in the presence of molecular sieve catalyst,
Contained alkene in catalytic pyrolysis raw material obtains a kind of method of light molecular olefine propylene and ethylene.It is representative at present
Several olefins by catalytic cracking techniques mainly have：Propylur techniques, OCP techniques, Omega techniques, OCC techniques and Superflex
Technique.Propylur techniques are developed by German Lurgi companies, using fixed bed reaction technique, by the use of steam as dilution raw material, are adopted
With molecular sieve catalyst, the adiabatic progress under 500 DEG C, 0~0.1MPaG is reacted, reactor is fixed bed pattern, and two to open one standby；
Between 0.5~3.0, catalyst life reaches 15 months for the ratio between steam and raw material.The olefin conversion of Propylur techniques reaches
To 85%, once-through propylene yield 40mol%, yield of ethene 10mol% (relative to alkene total amount in charging)；This technique is in Germany
Worringen has a set of demonstration plant, does not there is commercial plant construction also at present.OCP techniques are cooperated out by UOP with Atofina
Hair, using fixed bed reaction technique, reacts and is carried out under 500~600 DEG C, 0.1~0.4MPaG；Using high-speed, without carrier gas
The reaction system of body.Omega techniques are developed by the Asahi Kasei Corporation of Japan, are reacted and are carried out in single hop, adiabatic fixed bed, by
Two reactor switchings regenerate catalyst；Using molecular sieve catalyst, react in 530~600 DEG C, 0~0.5MPaG
Under the conditions of carry out, reaction velocity WHSV be 3~10h-1, this technique olefin conversion be more than 75%.Asahi Chemical Industry is in June, 2006
The device of a set of Omega methods production propylene has been built on water island.OCC techniques are developed by Shanghai Petroleum Chemical Engineering Institute, are reacted
It is adiabatic in fixed bed to carry out.Using a kind of technique of no diluent gas, reaction velocity WHSV is 15~30h-1, reaction pressure 0
~0.15MPaG, reaction temperature are 500~560 DEG C, and alkene conversion per pass is more than 65%.OCC techniques are at the beginning of 2004 upper
Extra large petrochemical industry limited company has built up the pilot-plant of 100 tons/year of scales.2009, in Central Plains, petrochemical industry Co., Ltd built up
Scale is 60,000 tons/year of OCC commercial plants.
Industrialized triolefin technique is often its back reaction, i.e.,：The technique of ethylene and butene reaction production propylene, in second
During allyl alkene price inversion have good economy, once but ethylene, propylene price do not hang upside down, economy offset sharper slowdowns.Together
When the technology to raw material be C5+ alkene when adaptability it is bad, yield be not so good as C4 alkene.
Olefins by catalytic cracking technology has the advantages that adaptability to raw material is good, ethylene, propylene high income, not consumption of ethylene, but
Be often there are yield of ethene is low, E/P than it is unadjustable the shortcomings of.
Utility model content
Technical problem to be solved in the utility model be E/P in the prior art it is smaller than adjustable amplitude, to second
Alkene and the adaptability of propylene price fluctuation is not strong, yield of ethene is low；E/P ratios in particularly existing MTO technologies, MTO+OCC technologies
Adjustable the problem of amplitude is small, yield of ethene is low, the device of a kind of new production ethylene and propylene is provided, which has E/
P is bigger than adjustable amplitude, to ethylene and the adaptable of propylene price fluctuation, yield of ethene it is high, especially suitable for ethylene and third
The advantages that alkene price difference is at+500 yuan/ton.
In order to solve the above technical problems, the technical solution adopted in the utility model is as follows：A kind of ethylene and propylene of producing
Device divides in advance including olefin cracking reaction member A, olefin cracking pre-separation unit B, olefin dismutation reaction unit C, olefin(e) disproportionation
From cells D, the hydrocarbon pyrolysis reaction member A is used for catalytic pyrolysis hydrocarbon mixture；Olefin cracking pre-separation unit B is used to detach alkene
C caused by the hydrocarbon pyrolysis3Component, ethane, C4~C6Component and other components；Olefin dismutation reaction unit C is used for propylene
It is disproportionated into ethylene and butylene；Olefin(e) disproportionation pre-separation cells D is used to detach unreacted C3Caused by component and olefin(e) disproportionation
Ethylene and C4+ component, it is characterised in that：The outlet of olefin cracking reaction member A is connected to olefin cracking pre-separation unit B,
By the C of olefin cracking pre-separation unit B3Outlet is connected to olefin dismutation reaction unit C, by the C of olefin dismutation reaction unit C4+
Outlet port is connected to olefin cracking reaction member A entrances.
In above-mentioned technical proposal, it is preferred that olefin cracking pre-separation unit B includes at least a depropanizing tower.
In above-mentioned technical proposal, it is preferred that olefin cracking pre-separation unit B includes at least a dethanizer.
In above-mentioned technical proposal, it is preferred that olefin(e) disproportionation pre-separation cells D includes at least an ethylene rectifying column.
In above-mentioned technical proposal, it is preferred that olefin(e) disproportionation pre-separation cells D includes at least a de- C3Tower.
In above-mentioned technical proposal, it is preferred that depropanizing tower tower top outlet and deethanization in olefin cracking pre-separation unit B
Tower import is connected.
In above-mentioned technical proposal, it is preferred that the ethylene rectifying column tower reactor of olefin(e) disproportionation pre-separation cells D weight exports and take off C3
Tower import is connected.
In the art, there is the related industries report of inverse disproportionation, there is no the industry reports being just disproportionated.General technology
Personnel less will recognize that the combination using positive disproportionated reaction unit and other techniques to realize good technique effect.
Using the device of the utility model, by the combination of olefin cracker and olefin(e) disproportionation unit, it can be achieved that E/P ratios
It is adjusted in being adjusted 0.25~15, and its E/P of conventional equipment is substantially unadjustable (as used reverse disproportionated reaction, E/P ratios
It is negative, i.e. consumption of ethylene；Such as using olefins by catalytic cracking technique, the E/P ratios that are averaged are about 0.3 or so).Spy more than having
Property, the utility model have the advantages that high to ethylene and the adaptable of propylene price fluctuation, yield of ethene.
The utility model is further elaborated below by embodiment.
Description of the drawings
Fig. 1 is the process flow diagram of the utility model.
A is olefin cracking reaction member；
B is olefin cracking pre-separation unit；
C is olefin dismutation reaction unit；
D is olefin(e) disproportionation pre-separation unit；
1 is the conveyance conduit of olefin cracker raw material (olefin-containing logistics)；
2 be the separated conveyance conduit containing ethylene streams of olefin cracking pre-separation unit；
The conveyance conduit of 3 other products separated for olefin cracking pre-separation unit；
4 Cs separated for olefin cracking pre-separation unit3The conveyance conduit of logistics；
5 conveyance conduits containing propylene stream (send part) separated for olefin cracking pre-separation unit；
6 conveyance conduits containing propylene stream (be sent into olefin(e) disproportionation part) separated for olefin cracking pre-separation unit；
The conveyance conduit of 7 ethylene streams separated for olefin(e) disproportionation pre-separation unit；
The conveyance conduit of 8 propylene streams separated for olefin(e) disproportionation pre-separation unit；
The conveyance conduit of the 9 C4+ logistics separated for olefin(e) disproportionation pre-separation unit；
10 be the conveyance conduit of olefin cracking reaction member outlet streams；
11 be the conveyance conduit of olefin dismutation reaction unit outlet streams；
Hydrocarbon material flow 1 and cycle logistics 9 are sent into A units, olefin cracking reaction occurs, generates lighter hydrocarbons, ethylene, propylene
And heavy hydrocarbon, it is separated into the logistics 2 containing ethylene, the logistics 3 containing heavy hydrocarbon and the logistics rich in propylene ingredient by B
4, all or part of feeding C cell of logistics 4, when II units are sent into 4 part of logistics, logistics 5 is as outer rich in propylene
Arrange logistics.After being sent into II units reaction of the propylene disproportionation into ethylene and butylene occurs for the logistics 6 rich in propylene, it is passed through D points
Ethylene product stream 7, unreacted propylene stream 8 and C4+ logistics 9 are obtained from after, the C4+ logistics 9 that II units generate is recycled
It returns in A.
Fig. 2 is a kind of thin portion process flow diagram of preferred embodiment of the utility model.
B is olefin cracking pre-separation unit；
C is olefin dismutation reaction unit；
A is depropanizing tower；
B is dethanizer；
C is de- ethylene column；
2 be the separated conveyance conduit containing ethylene streams of olefin cracking pre-separation unit；
4 Cs separated for olefin cracking pre-separation unit3The conveyance conduit of logistics；
10 be the conveyance conduit of olefin cracking reaction member outlet streams；
Olefin cracking reaction member is exported and is sent into B through conveyance conduit 5, comprising a, b, c in B, wherein a overhead streams into
Enter in b, b overhead streams enter c, and b bottoms enter in C, and c bottoms enter in F.
Fig. 3 is a kind of thin portion process flow diagram of preferred embodiment of the utility model.
D is olefin(e) disproportionation pre-separation unit；
F is steam cracking furnace；
D is ethylene rectifying column；
E is de- C3Tower；
The conveyance conduit of 7 ethylene streams separated for olefin(e) disproportionation pre-separation unit；
8 Cs separated for olefin(e) disproportionation pre-separation unit3The conveyance conduit of logistics；
11 be the conveyance conduit of olefin dismutation reaction unit outlet streams；
Olefin dismutation reaction unit outlet streams through conveyance conduit 6 and are sent into D, d, e, wherein e headpieces are included in D
Stream enters in F, and d top exits and 7 are connected.
Specific embodiment
【Embodiment 1】
Using flow shown in FIG. 1, the C5 alkene containing 50% C4 alkene, 20% in logistics 1,15% C6 alkene,
10% C7 alkene, 5% C8 alkene, total flow 1000kg/h.By logistics caused by I 4, (its flow is 1021kg/
H, propylene content 86%) II is sent into, the mass fraction of logistics 4 shared by logistics 6 is 100%；By 9 (its of logistics caused by II
Flow is 553kg/h, and wherein 96%) C4 olefin(e) centents is return to I.
The logistics containing target product is 2,7,8 in obtained product, wherein containing 291kg/h ethylene in 2, is contained in 7
There is 277kg/h ethylene, the propylene containing 43kg/h in 8.Overall ethylene+propene yield is 62.0%, and ethylene/propene ratio is
13.2.Specific data are shown in Table 1.
【Embodiment 2】
Using flow shown in FIG. 1, the C5 alkene containing 50% C4 alkene, 20% in logistics 1,15% C6 alkene,
10% C7 alkene, 5% C8 alkene, flow 1000kg/h.By logistics caused by I 4 (its flow be 968kg/h,
Propylene content is that 85.6%) II is sent into part, and the mass fraction of logistics 4 shared by logistics 6 is 90%；By logistics 9 caused by II
(its flow is 472kg/h, and wherein 96%) C4 olefin(e) centents is return to I.
The logistics containing target product contains 276kg/h ethylene in obtained product in being 2,5,7,8 wherein 2, contains in 5
There is a propylene of 83kg/h, containing 236kg/h ethylene in 7, the propylene containing 38kg/h in 8.Overall ethylene+propene yield is
63.3%, ethylene/propene ratio is 4.2.Specific data are shown in Table 1.
【Embodiment 3】
Using flow shown in FIG. 1, the C5 alkene containing 50% C4 alkene, 20% in logistics 1,15% C6 alkene,
10% C7 alkene, 5% C8 alkene, flow 1000kg/h.By logistics caused by I 4 (its flow be 876kg/h,
Propylene content is that 85.4%) II is sent into part, and the mass fraction of logistics 4 shared by logistics 6 is 70%；By logistics 9 caused by II
(its flow is 332kg/h, and wherein 95%) C4 olefin(e) centents is return to I.
The logistics containing target product contains 250kg/h ethylene in obtained product in being 2,5,7,8 wherein 2, contains in 5
There is a propylene of 225kg/h, containing 166kg/h ethylene in 7, the propylene containing 26kg/h in 8.Overall ethylene+propene yield is
66.7%, ethylene/propene ratio is 2.5.Specific data are shown in Table 1.
【Embodiment 4】
Using flow shown in FIG. 1, the C5 alkene containing 50% C4 alkene, 20% in logistics 1,15% C6 alkene,
10% C7 alkene, 5% C8 alkene, flow 1000kg/h.By logistics caused by I 4 (its flow be 800kg/h,
Propylene content is that 86.2%) II is sent into part, and the mass fraction of logistics 4 shared by logistics 6 is 50%；By logistics 9 caused by II
(its flow is 217kg/h, and wherein 95%) C4 olefin(e) centents is return to I.
The logistics containing target product contains 228kg/h ethylene in obtained product in being 2,5,7,8 wherein 2, contains in 5
There is a propylene of 342kg/h, containing 108kg/h ethylene in 7, the propylene containing 17kg/h in 8.Overall ethylene+propene yield is
69.8%, ethylene/propene ratio is 0.88.Specific data are shown in Table 1.
【Embodiment 5】
Using flow shown in FIG. 1, the C5 alkene containing 50% C4 alkene, 20% in logistics 1,15% C6 alkene,
10% C7 alkene, 5% C8 alkene, flow 1000kg/h.By logistics caused by I 4 (its flow be 736kg/h,
Propylene content is that 85.8%) II is sent into part, and the mass fraction of logistics 4 shared by logistics 6 is 30%；By logistics 9 caused by II
(its flow is 119kg/h, and wherein 96%) C4 olefin(e) centents is return to I.
The logistics containing target product contains 210kg/h ethylene in obtained product in being 2,5,7,8 wherein 2, contains in 5
There is a propylene of 441kg/h, containing 60kg/h ethylene in 7, the propylene containing 9kg/h in 8.Overall ethylene+propene yield is
72.0%, ethylene/propene ratio is 0.6.Specific data are shown in Table 1.
【Embodiment 6】
Using flow shown in FIG. 1, the C5 alkene containing 50% C4 alkene, 20% in logistics 1,15% C6 alkene,
10% C7 alkene, 5% C8 alkene, flow 1000kg/h.By logistics caused by I 4 (its flow be 682kg/h,
Propylene content is that 85.6%) II is sent into part, and the mass fraction of logistics 4 shared by logistics 6 is 10%；By logistics 9 caused by II
(its flow is 37kg/h, and wherein 96%) C4 olefin(e) centents is return to I.
The logistics containing target product contains 194kg/h ethylene in obtained product in being 2,5,7,8 wherein 2, contains in 5
There is a propylene of 525kg/h, containing 19kg/h ethylene in 7, the propylene containing 3kg/h in 8.Overall ethylene+propene yield is
74.1%, ethylene/propene ratio is 0.4.Specific data are shown in Table 1.
【Embodiment 7】
Using flow shown in FIG. 1, the C5 alkene containing 50% C4 alkene, 20% in logistics 1,15% C6 alkene,
10% C7 alkene, 5% C8 alkene, flow 1000kg/h.By logistics caused by I 4 (its flow be 658kg/h, third
Alkene content is sent into II for 85.5%) part, and the mass fraction of logistics 4 shared by logistics 6 is 0.1%；By logistics 9 caused by II
(its flow is 0.4kg/h, and wherein 96%) C4 olefin(e) centents is return to I.
The logistics containing target product contains 188kg/h ethylene in obtained product in being 2,5,7,8 wherein 2, contains in 5
There is a propylene of 562kg/h, containing 0.18kg/h ethylene in 7, the propylene containing 0.01kg/h in 8.Overall ethylene+propene yield is
75.0%, ethylene/propene ratio is 0.33.Specific data are shown in Table 1.
Table 1
。
Claims (10)
1. a kind of device for producing ethylene and propylene, including olefin cracking reaction member A, olefin cracking pre-separation unit B, alkene
Disproportionated reaction unit C, olefin(e) disproportionation pre-separation cells D, the hydrocarbon pyrolysis reaction member A are used for catalytic pyrolysis hydrocarbon mixture；Alkene
Hydrocarbon pyrolysis pre-separation unit B is used to detach C caused by olefin cracking3Component, ethane, C4~C6Component and other components；Alkene
Hydrocarbon dismutation reaction member C is used for propylene disproportionation into ethylene and butylene；Olefin(e) disproportionation pre-separation cells D is unreacted for detaching
C3Ethylene and C caused by component and olefin(e) disproportionation4+ component, it is characterised in that：The outlet of olefin cracking reaction member A is connected
To olefin cracking pre-separation unit B, by the C of olefin cracking pre-separation unit B3Outlet is connected to olefin dismutation reaction unit C, will
The C of olefin dismutation reaction unit C4+ outlet port is connected to olefin cracking reaction member A entrances.
2. the device of production ethylene according to claim 1 and propylene, it is characterised in that olefin cracking pre-separation unit B is extremely
A depropanizing tower is included less.
3. the device of production ethylene according to claim 1 and propylene, it is characterised in that olefin cracking pre-separation unit B is extremely
A dethanizer is included less.
4. the device of production ethylene according to claim 1 and propylene, it is characterised in that olefin(e) disproportionation pre-separation cells D is extremely
An ethylene rectifying column is included less.
5. the device of production ethylene according to claim 1 and propylene, it is characterised in that olefin(e) disproportionation pre-separation cells D is extremely
A de- C is included less3Tower.
6. according to Claims 2 or 3 production ethylene and propylene device, it is characterised in that depropanizing tower tower top outlet and
Dethanizer import is connected.
7. the device of production ethylene according to claim 4 or 5 and propylene, it is characterised in that ethylene rectifying column tower reactor exports
With de- C3Tower import is connected.
8. a kind of device combination for producing polyethylene, it is characterised in that including any one of claim 1~7 described device.
9. a kind of polyacrylic device combination of production, it is characterised in that including any one of claim 1~7 described device.
10. a kind of combine for producing the device of ethene derivatives or acryloyl derivative, it is characterised in that including claim 1~
Any one of 7 described devices.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721126382.8U CN207468520U (en) | 2017-09-04 | 2017-09-04 | Produce the device of ethylene and propylene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721126382.8U CN207468520U (en) | 2017-09-04 | 2017-09-04 | Produce the device of ethylene and propylene |
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| CN207468520U true CN207468520U (en) | 2018-06-08 |
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| CN201721126382.8U Active CN207468520U (en) | 2017-09-04 | 2017-09-04 | Produce the device of ethylene and propylene |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019042449A1 (en) * | 2017-09-04 | 2019-03-07 | 中国石油化工股份有限公司 | Process for producing ethylene |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019042449A1 (en) * | 2017-09-04 | 2019-03-07 | 中国石油化工股份有限公司 | Process for producing ethylene |
| US11091412B2 (en) | 2017-09-04 | 2021-08-17 | China Petroleum & Chemical Corporation | Process for producing ethylene |
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