CN207347429U - The preparation facilities of ethene - Google Patents
The preparation facilities of ethene Download PDFInfo
- Publication number
- CN207347429U CN207347429U CN201721126345.7U CN201721126345U CN207347429U CN 207347429 U CN207347429 U CN 207347429U CN 201721126345 U CN201721126345 U CN 201721126345U CN 207347429 U CN207347429 U CN 207347429U
- Authority
- CN
- China
- Prior art keywords
- olefin
- ethene
- unit
- cracking
- disproportionation
- 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.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The purpose of this utility model is that solve the problems, such as that current ethylene unit yield of ethene is low, provide a kind of preparation facilities of New Type of Ethylene, by using including olefin cracking reaction member A, the device that olefin cracking pre-separation unit B, olefin dismutation reaction unit C, olefin(e) disproportionation pre-separation cells D, full hydrogenation unit E and steam cracking furnace F are formed, there is yield of ethene height, good economy performance, available for supporting ethylene unit, especially suitable for naphtha cracker complex.
Description
Technical field
It the utility model is related to a kind of preparation facilities of ethene, and in particular to one kind utilizes catalysis and thermal cracker ethene
Preparation facilities.
Background technology
Triolefin technique (The Triolefin Process) is：Propylene disproportionation produces the ethene and butene-2 of high-purity；
With the back reaction of the reaction, ethene 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 ethene 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, afterwards 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 ethene.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 developed cooperatively by UOP and Atofina,
Using fixed bed reaction technique, react and carried out under 500~600 DEG C, 0.1~0.4MPaG；Using high-speed, without diluent gas
Reaction system.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
A reactor switching regenerates catalyst；Using molecular sieve catalyst, react in 530~600 DEG C, 0~0.5MPaG conditions
Lower progress, reaction velocity WHSV are 3~10h-1, this technique olefin conversion is more than 75%.Asahi Chemical Industry is in June, 2006 in water
The device of a set of Omega methods production propylene is built in island.OCC techniques are developed by Shanghai Petroleum Chemical Engineering Institute, are reacted in fixation
It is adiabatic in bed to carry out.Using a kind of technique of no diluent gas, reaction velocity WHSV is 15~30h-1, reaction pressure be 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 in Shanghai
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.
Utility model content
The purpose of this utility model is that solve the problems, such as that current ethylene unit yield of ethene is low, there is provided a kind of new second
The preparation facilities of alkene, when which is used to produce ethene, has the advantages that yield of ethene height, good economy performance.
Industrialized triolefin technique, is often its back reaction, i.e.,：The technique of ethene and butene reaction production propylene, in second
With good economy during allyl alkene price inversion, once but ethylene, propylene price do not hang upside down, economy offset sharper slowdowns.Together
When the technology it is bad to adaptability when raw material is C5+ alkene, yield is not so good as C4 alkene.
Industrialized olefins by catalytic cracking technology, there is good adaptability to raw material, not ethylene, propylene high income, consumption of ethylene etc.
Advantage, but often there are yield of ethene is low, E/P than it is unadjustable the shortcomings of.
For the steam cracking device using naphtha as raw material, the carbon four of by-product is after alkadienes butene-1 is extracted toward outward
Sell, the utilization of light dydrocarbon hydro carbons it is more few, majority be used for fuel take out.
In recent years there is the technology path that remaining carbon four and light dydrocarbon are hydrogenated with entirely and return to pyrolysis furnace, with further lifting cracking dress
The yield of ethene put, but often yield is not high, below 45%.
Technical problem to be solved in the utility model is the problem of yield of ethene existing in the prior art is low, there is provided
A kind of technical solution of new production ethene, compared to conventional solution, the technical program yield of ethene can reach 60% with
On, it is especially suitable for steam cracking device of the lifting using naphtha as raw material.
In order to solve the above technical problems, the technical solution adopted in the utility model is as follows：A kind of preparation facilities of ethene, bag
Include olefin cracking reaction member A, olefin cracking pre-separation unit B, olefin dismutation reaction unit C, olefin(e) disproportionation pre-separation unit
D, full hydrogenation unit E and steam cracking furnace F, the olefin cracking reaction member A are used for catalytic pyrolysis hydrocarbon mixture；Olefin cracking
Pre-separation unit B is used to separate C caused by olefin cracking3Component, ethane, C4~C6Component and other components；Olefin(e) disproportionation
Reaction member C is used for propylene disproportionation into ethene and butylene；Olefin(e) disproportionation pre-separation cells D is used to separate unreacted C3Component
And ethene caused by olefin(e) disproportionation and C4+ component；Full hydrogenation unit E is used for alkene saturation into alkane；Steam cracking furnace F is used
In thermal cracking of hydrocarbons, it is characterised in that：The outlet of olefin cracking reaction member A is connected to olefin cracking pre-separation unit B, will
The C of olefin cracking pre-separation unit B3Outlet is connected to olefin dismutation reaction unit C, by the outlet of olefin dismutation reaction unit C
Olefin(e) disproportionation pre-separation cells D is connected to, by the C of D4+ outlet port is connected to olefin cracking reaction member A entrances, by alkene discrimination
Change unreacted C in pre-separation cells D3Component outlet port, the C of olefin cracking pre-separation unit B4~C6Outlet port and full hydrogenation are single
First E entrances are connected, by the outlet of the ethane outlet port of olefin cracking pre-separation unit B and full hydrogenation unit E and steam cracking
Stove F entrances are connected.
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 cracking pre-separation unit B includes at least a de- ethylene column.
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 is connected with dethanizer import.
In above-mentioned technical proposal, it is preferred that deethanizer overhead exports and takes off ethylene column import and be connected.
In above-mentioned technical proposal, it is preferred that de- ethylene column tower reactor outlet is connected with steam cracking furnace F.
In above-mentioned technical proposal, it is preferred that ethylene rectifying column tower reactor exports and take off C3Tower import is connected.
In above-mentioned technical proposal, it is preferred that de- C3Column overhead outlet is connected with full hydrogenation unit E imports.
Using the device of the utility model, pass through olefin cracker, olefin(e) disproportionation unit, hydrogenation unit and pyrolysis furnace
Combination can realize high yield of ethene, obtain good technique effect.
The utility model is further elaborated below by embodiment.
Brief description of the drawings
Fig. 1 is a kind of process flow diagram of preferred solution 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；
E is full hydrogenation unit；
F is steam cracking furnace；
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；
3 be the conveyance conduit of other separated products of olefin cracking pre-separation unit；
4 be the separated C of olefin cracking pre-separation unit3The conveyance conduit of logistics；
5 be the conveyance conduit of olefin cracking reaction member outlet streams；
6 be the conveyance conduit of olefin dismutation reaction unit outlet streams；
7 be the conveyance conduit of the separated ethylene streams of olefin(e) disproportionation pre-separation unit；
8 be the separated C of olefin(e) disproportionation pre-separation unit3The conveyance conduit of logistics；
9 be the separated C of olefin(e) disproportionation pre-separation unit4The conveyance conduit of+logistics；
10 be the conveyance conduit of the separated ethane of olefin cracking pre-separation unit；
11 be the conveyance conduit of gained logistics after full hydrogenation；
12 be conveyance conduit of the gained containing ethylene streams after steam cracking；
13 be the separated C of olefin cracking pre-separation unit4~C6The conveyance conduit of logistics；
Hydrocarbon material flow 1 and circulation logistics 9 are sent into A, olefin cracking reaction occurs, produces lighter hydrocarbons, ethene, ethane, third
Alkene, C4~C6With the logistics 5 of heavy hydrocarbon, 5 are sent into B, is separated into the logistics 2 containing ethene, the logistics 3 containing heavy hydrocarbon, richness
The logistics 4 and ethane 10 of the component containing propylene, containing C4~C6Logistics 13, logistics 4 is sent into C, and propylene disproportionation generation occurs and contains second
The logistics 6 of alkene and butylene, will obtain ethylene product stream 7, unreacted propylene stream 8 and C after 6 feeding D separation4+ logistics 9,
Logistics 9 is recycled back to A, 8,13 are sent into E and obtains 11, F is sent into logistics 11 and logistics 10, obtain containing ethylene streams 12.
Fig. 2 is a kind of thin portion process flow diagram of preferred solution of the utility model.
B is olefin cracking pre-separation unit；
C is olefin dismutation reaction unit；
F is steam cracking furnace；
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 be the separated C of olefin cracking pre-separation unit3The conveyance conduit of logistics；
5 be the conveyance conduit of olefin cracking reaction member outlet streams；
10 be the conveyance conduit of the separated ethane of olefin cracking pre-separation unit；
Olefin cracking reaction member is exported and is sent into B through conveyance conduit 5, includes 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 solution 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；
6 be the conveyance conduit of olefin dismutation reaction unit outlet streams；
7 be the conveyance conduit of the separated ethylene streams of olefin(e) disproportionation pre-separation unit；
8 be the separated C of olefin(e) disproportionation pre-separation unit3The conveyance conduit of logistics；
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.
Fig. 4 is the process flow diagram of conventional solution.
E is hydrogenation unit；
F is steam cracking furnace
The conveyance conduit of the hydrocarbon material flow of 1 olefin-containing；
12 be conveyance conduit of the gained containing ethylene streams after steam cracking.
Hydrocarbon material flow 1 is sent into steam cracking furnace IV after hydrogenation unit III, steam cracking furnace obtains containing ethylene streams
12。
Embodiment
【Embodiment 1】
Using the flow shown in Fig. 1：
C5 alkene containing 50% C4 alkene, 20%, 15% C6 alkene, 5% C7 alkene, 5% C8 in logistics 1
Alkene, 5% C4 alkane, its total flow are 1000kg/h.
A is sent into logistics 1 and produces logistics 5, logistics 5 is separated into effluent stream 2,3,4,10,13 by B, by (its flow of logistics 4
For 970kg/h, propylene content 93.4%) all be sent into be sent into C obtain logistics 6, isolated logistics in D is sent into logistics 6
7th, 8,9, by logistics 9, (its flow is 628kg/h, and wherein C4 olefin(e) centents return to A to be 96%) whole.
F is all sent into logistics 8,13 after E, logistics 10 is all sent into F, produces the logistics 12 containing ethene.
The logistics containing target product is 2,7,12 in obtained product, wherein 2 ethene containing 302kg/, is contained in 7
There is 301kg/h ethene, contain 122kg/h ethene in 12.Overall yield of ethene is 72.5%.
【Embodiment 2】
Using the flow shown in Fig. 1：
C5 alkene containing 60% C4 alkene, 25% in logistics 1,10% C6 alkene, 3% C4 alkane, 2% C5
Alkane, its total flow are 1000kg/h.
A is sent into logistics 1 and produces logistics 5, logistics 5 is separated into effluent stream 2,3,4,10,13 by B, by (its flow of logistics 4
For 970kg/h, propylene content 93.4%) all be sent into C obtain logistics 6, by logistics 6 be sent into isolated logistics 7 in D, 8,
9, by logistics 9, (its flow is 628kg/h, and wherein C4 olefin(e) centents return to A to be 96%) whole.
F is all sent into logistics 8,13 after E, logistics 10 is all sent into F, produces the logistics 12 containing ethene.
The logistics containing target product is 2,7,12 in obtained product, wherein 2 ethene containing 308kg/, is contained in 7
There is 306kg/h ethene, contain 124kg/h ethene in 12.Overall yield of ethene is 73.8%.
【Comparative example 1】
Using the flow shown in Fig. 2：
C5 alkene containing 50% C4 alkene, 25% in logistics 1,5% C6 alkene, 15% C4 alkane, 5% C5
Alkane, its total flow are 1000kg/h.
F is all sent into logistics 1 after E, produces the logistics 12 containing ethene.
The logistics containing target product is 12 in obtained product, wherein containing 675kg/h ethene.Overall yield of ethene
For 45.0%.
Claims (11)
1. a kind of preparation facilities of ethene, including olefin cracking reaction member A, olefin cracking pre-separation unit B, olefin(e) disproportionation are anti-
Answer unit C, olefin(e) disproportionation pre-separation cells D, full hydrogenation unit E and steam cracking furnace F, the olefin cracking reaction member A use
In catalytic pyrolysis hydrocarbon mixture；Olefin cracking pre-separation unit B is used to separate C caused by olefin cracking3Component, ethane, C4~
C6Component and other components；Olefin dismutation reaction unit C is used for propylene disproportionation into ethene and butylene；Olefin(e) disproportionation pre-separation
Cells D is used to separate unreacted C3Ethene and C caused by component and olefin(e) disproportionation4+ component；Full hydrogenation unit E is used for alkene
Hydrocarbon saturation is into alkane；Steam cracking furnace F is used for thermal cracking of hydrocarbons, it is characterised in that：The outlet of olefin cracking reaction member A is connected
Olefin cracking pre-separation unit B is connected to, by the C of olefin cracking pre-separation unit B3Outlet is connected to olefin dismutation reaction unit C,
The outlet of olefin dismutation reaction unit C is connected to olefin(e) disproportionation pre-separation cells D, by the C of D4+ outlet port is connected to alkene and splits
Reaction member A entrances are solved, by unreacted C in olefin(e) disproportionation pre-separation cells D3Component outlet port, olefin cracking pre-separation unit B
C4~C6Outlet port is connected with full hydrogenation unit E entrances, by the ethane outlet port of olefin cracking pre-separation unit B and it is complete plus
The outlet of hydrogen unit E is connected with steam cracking furnace F entrances.
2. the preparation facilities of ethene according to claim 1, it is characterised in that olefin cracking pre-separation unit B includes at least
One depropanizing tower.
3. the preparation facilities of ethene according to claim 1, it is characterised in that olefin cracking pre-separation unit B includes at least
One dethanizer.
4. the preparation facilities of ethene according to claim 1, it is characterised in that olefin cracking pre-separation unit B includes at least
One de- ethylene column.
5. the preparation facilities of ethene according to claim 1, it is characterised in that olefin(e) disproportionation pre-separation cells D includes at least
One ethylene rectifying column.
6. the preparation facilities of ethene according to claim 1, it is characterised in that olefin(e) disproportionation pre-separation cells D includes at least
One de- C3Tower.
7. the preparation facilities of the ethene according to Claims 2 or 3, it is characterised in that depropanizing tower tower top outlet and deethanization
Tower import is connected.
8. the preparation facilities of the ethene according to claim 3 or 4, it is characterised in that deethanizer overhead exports and take off ethene
Tower import is connected.
9. the preparation facilities of ethene according to claim 4, it is characterised in that de- ethylene column tower reactor outlet and steam cracking
Stove F is connected.
10. the preparation facilities of the ethene according to claim 5 or 6, it is characterised in that ethylene rectifying column tower reactor exports and take off C3
Tower import is connected.
11. the preparation facilities of ethene according to claim 6, it is characterised in that de- C3Column overhead exports and full hydrogenation unit E
Import is connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721126345.7U CN207347429U (en) | 2017-09-04 | 2017-09-04 | The preparation facilities of ethene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721126345.7U CN207347429U (en) | 2017-09-04 | 2017-09-04 | The preparation facilities of ethene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207347429U true CN207347429U (en) | 2018-05-11 |
Family
ID=62413343
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721126345.7U Active CN207347429U (en) | 2017-09-04 | 2017-09-04 | The preparation facilities of ethene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207347429U (en) |
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 |
-
2017
- 2017-09-04 CN CN201721126345.7U patent/CN207347429U/en active Active
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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101165017B (en) | Production increasing method for propylene | |
| CN101279879B (en) | Method for producing propone by comprehensive utilization of mixed C4 | |
| CN101165025B (en) | Method for producing ethylene and propylene from methanol or dimethyl ether | |
| CN102372573B (en) | Method for preparing propylene by using etherified C4 and ethylene | |
| CN101165026B (en) | Method for producing ethylene and propylene from methanol and dimethyl ether | |
| CN111423302B (en) | Method and device for preparing olefin from methanol | |
| CN101165018A (en) | Method for producing ethylene and propylene | |
| CN106478351A (en) | Iso-butane and/or the method for dehydrogenating propane | |
| CN101935265B (en) | Liquefied gas catalytic pyrolysis process | |
| CN103121892A (en) | Method for producing low-carbon olefin by alkane | |
| CN207347425U (en) | Prepare the device of ethene | |
| CN207347428U (en) | The process units of ethene | |
| CN101891576A (en) | Process and device for preparing low-carbon olefin by methanol and/or dimethyl ether | |
| CN101585747B (en) | Method for transforming oxygenates into propylene | |
| CN102268286A (en) | C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device | |
| CN207347429U (en) | The preparation facilities of ethene | |
| CN101165020B (en) | Method for increasing yield of propylene | |
| CN101165019B (en) | Method for producing ethylene and propylene | |
| CN101165027B (en) | Method for producing ethylene and propylene from oxygen-containing compounds | |
| CN207342677U (en) | Produce the device of ethene | |
| CN207468520U (en) | Produce the device of ethylene and propylene | |
| CN104557362B (en) | Methanol and/or dimethyl ether conversion aromatic hydrocarbons coproduction ethylene, the system and method for propylene | |
| CN103694077B (en) | A kind of propylene that produces can the reaction process of coproduction high octane gasoline component | |
| CN103772117A (en) | Method for preparing butadiene through multistage adiabatic oxidative dehydrogenation of butylene | |
| CN109422610B (en) | Method for increasing yield of ethylene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |