CN106008131A - Energy-saving equipment and production process for producing MTBE with butane in heterogeneous co-production mode - Google Patents
Energy-saving equipment and production process for producing MTBE with butane in heterogeneous co-production mode Download PDFInfo
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- CN106008131A CN106008131A CN201610451238.5A CN201610451238A CN106008131A CN 106008131 A CN106008131 A CN 106008131A CN 201610451238 A CN201610451238 A CN 201610451238A CN 106008131 A CN106008131 A CN 106008131A
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- alkane
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- olefin
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
- C07C5/2767—Changing the number of side-chains
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
- C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
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- 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
- Y02P20/10—Process efficiency
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Abstract
The invention provides energy-saving equipment and a production process for producing MTBE with butane in a heterogeneous co-production mode. The equipment comprises a heterogeneous reactor, a compressor, an alkane olefin separation tower, an alkane olefin separation tower condenser, an alkane olefin separation tower return tank, an alkane olefin separation tower reboiler and an MTBE unit; the process includes the steps that olefin components are subjected to isobutene concentration extraction and n-butene concentration extraction respectively through the alkane olefin separation tower, isobutene obtained after concentration extraction is sent to an MTBE production device, and n-butene returns to an inlet of the heterogeneous reactor. The energy-saving equipment and the production process have the advantages that materials at the top of the separation tower are sent to the MTBE unit, lateral line butane is returned to the inlet of the heterogeneous reactor, and light dydrocarbon at the bottom of the tower is exploited out. Due to the fact that an outlet of the compressor is provided with a gas phase, the gas phase enters the alkane olefin separation tower directly, steam consumption of the separation tower is saved, energy consumption of separating isobutene from n-butene is lowered, heat of the fed gas phase is fully utilized, steam consumption caused by component backmixing is lowered, and operation cost is greatly lowered by adding a lateral line exploiting and recycling system of the separation tower compared with traditional alkanes olefin separation.
Description
Technical field
The present invention relates to petrochemical industry, particularly relate to the energy-saving equipment of a kind of butylene isomery coproduction MTBE and produce work
Skill.
Background technology
Before existing isomerization of butene production technology, being furnished with alkane alkene extraction equipment, isomerization product many employings weight-removing column enters more
Row separation of carbon four and lighter hydrocarbons, tower top carbon four component enters MTBE device, and after the by-product ether of MTBE device, carbon four is back to alkane alkene
Separative element, it is achieved alkane and the separation of alkene, the alkene after separation enters isomerization of butene unit, continues to produce isobutene..
Tradition separation of alkane and olefin device, uses the mode of extract and separate, and plant investment is high, and thermic load is big, after applying this technology, it is possible to maximum
The alkene that realizes of degree utilizes, and reduces plant investment, reduces device operating cost.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art, the present invention provides the butylene isomery coproduction of a kind of low energy consumption, Low investment
The energy-saving equipment of MTBE, it is characterised in that include isomerizing reactor, compressor, separation of alkane and olefin tower, separation of alkane and olefin tower condenser, alkane
Alkene knockout tower return tank, separation of alkane and olefin tower reboiler and MTBE unit, described isomerizing reactor exports through compressor with described
Separation of alkane and olefin tower charging aperture connects, and described separation of alkane and olefin tower gas outlet is connected with the air intake of described separation of alkane and olefin tower condenser,
The liquid outlet of described separation of alkane and olefin tower condenser and described separation of alkane and olefin tower return tank charging aperture, described separation of alkane and olefin tower return tank
Discharging opening is connected with upper refluxing opening, the MTBE unit of described separation of alkane and olefin tower, is positioned at the liquid outlet at the bottom of described separation of alkane and olefin tower tower
Being connected with fluid inlet, the lighter hydrocarbons extraction mouth of described separation of alkane and olefin tower reboiler, the lime set of described separation of alkane and olefin tower reboiler goes out
Mouth is connected with the lower refluxing opening of described separation of alkane and olefin tower, and the liquid phase extraction mouth of described separation of alkane and olefin tower enters with described isomerizing reactor
Mouth connects.
The number of plates of described separation of alkane and olefin tower is 100 pieces, and the charging aperture of described separation of alkane and olefin tower is positioned at 35 pieces of Board positions, institute
The liquid phase extraction mouth stating separation of alkane and olefin tower is positioned at 90 pieces of Board positions.
A kind of energy-saving processing technique of butylene isomery coproduction MTBE, it is characterised in that:
The material of isomerizing reactor outlet, is mainly composed of isobutene., n-butene, iso-butane, normal butane, and this strand of material is compressed
Machine enters separation of alkane and olefin tower；
Separation of alkane and olefin column overhead extraction material, is mainly composed of isobutene., iso-butane and a small amount of n-butene, normal butane, this stock
Material is through separation of alkane and olefin tower condenser and separation of alkane and olefin tower return tank, and a part is back to separation of alkane and olefin tower, and another part enters
MTBE unit, with methanol by after etherification reaction, without isobutene. in carbon four after ether, this strand of raw material is as alkylation feed；
The material of the side line liquid phase extraction mouth of separation of alkane and olefin tower, is mainly composed of normal butane, n-butene, this burst of material parts circulation
To isomerizing reactor entrance, part extraction, after mixing with carbon after ether four, feed as alkyl plant；
Separation of alkane and olefin tower materials at bottom of tower, is mainly composed of lighter hydrocarbons, as product extraction.
The reflux ratio scope of separation of alkane and olefin tower is 2.5 5.5.
The invention has the beneficial effects as follows: MTBE unit delivered to by knockout tower tower top material, side line butylene is back to isomerization reaction
Device entrance, lighter hydrocarbons extraction at the bottom of tower.Owing to compressor outlet is gas phase, it is directly entered separation of alkane and olefin tower, saves the steam of knockout tower
Consume, reduce the energy consumption that isobutene. separates with n-butene, optimize the feed entrance point that separation of alkane and olefin tower is optimal, and then meet isobutyl
Alkene, iso-butane are from overhead extraction, and n-butene, normal butane, from side take-off, make full use of the heat of gas-phase feed, reduce component and return
The mixed steam consumption caused, by increasing side take-off and the blood circulation of knockout tower, compared with tradition separation of alkane and olefin, drops significantly
Low operating cost.Replace plant investment and the steam consumption quantity of separation of alkane and olefin, as a example by the isomerization of butene device of 600,000 tons,
The plant investment about 1.5 hundred million of alkane alkene extract and separate, fresh feed amount is 55t/h, and wherein olefin(e) centent is 60%, can steam saving
30t/h。
Accompanying drawing explanation
Fig. 1 is the structural representation of the energy-saving equipment of the present invention.
Detailed description of the invention
Below in conjunction with the accompanying drawings a kind of detailed description of the invention of the present invention is explained.
In figure, 1, isomerizing reactor；2, compressor；3, separation of alkane and olefin tower；4, separation of alkane and olefin tower condenser；5, separation of alkane and olefin
Tower return tank；6, separation of alkane and olefin tower reboiler；7, MTBE unit.
It is connected with described separation of alkane and olefin tower 3 charging aperture as it is shown in figure 1, described isomerizing reactor 1 exports through compressor 2,
Described separation of alkane and olefin tower 3 gas outlet is connected with the air intake of described separation of alkane and olefin tower condenser 4, described separation of alkane and olefin tower condenser
The liquid outlet of 4 and described separation of alkane and olefin tower return tank 5 charging aperture, described separation of alkane and olefin tower return tank 5 discharging opening and described alkane alkene
The upper refluxing opening of knockout tower 3, MTBE unit 7 connect, and are positioned at the liquid outlet at the bottom of described separation of alkane and olefin tower 3 tower and described separation of alkane and olefin
The fluid inlet of tower reboiler 6, lighter hydrocarbons extraction mouth connect, the condensate outlet of described separation of alkane and olefin tower reboiler 6 and described alkane alkene
The lower refluxing opening of knockout tower 3 connects, and the liquid phase extraction mouth of described separation of alkane and olefin tower 3 is connected with described isomerizing reactor 1 entrance.Institute
The number of plates stating separation of alkane and olefin tower 3 is 100 pieces, and the charging aperture of described separation of alkane and olefin tower is positioned at 35 pieces of Board positions, and described alkane alkene divides
Liquid phase extraction mouth from tower is positioned at 90 pieces of Board positions.
Production technology includes: the material of isomerizing reactor 1 outlet, is mainly composed of isobutene., n-butene, iso-butane, just
Butane, this strand of material enters separation of alkane and olefin tower 3 through compressor 2；
Separation of alkane and olefin tower 3 overhead extraction material, is mainly composed of isobutene., iso-butane and a small amount of n-butene, normal butane, should
Stock material is through separation of alkane and olefin tower condenser 4 and separation of alkane and olefin tower return tank 5, and a part is back to separation of alkane and olefin tower 3, another part
Entering MTBE unit 7, with methanol by after etherification reaction, without isobutene. in carbon four after ether, this strand of raw material is as alkylation feed；
The material of separation of alkane and olefin tower 3 side line liquid phase extraction mouth, is mainly composed of normal butane, n-butene, this burst of material parts circulation
To isomerizing reactor 1 entrance, part extraction, after mixing with carbon after ether four, feed as alkyl plant；
Separation of alkane and olefin tower 3 materials at bottom of tower, is mainly composed of lighter hydrocarbons, and part enters back into alkane alkene through separation of alkane and olefin tower reboiler 6 and divides
From tower 3, part is as product extraction.The reflux ratio scope of separation of alkane and olefin tower 3 is 2.5 5.5.
As a example by 600,000 tons/year of isomerization of butene projects, separation of alkane and olefin tower 3 pushes up product through separation of alkane and olefin tower condenser 4,
Condense to liquid phase, enter separation of alkane and olefin tower return tank 5.The alkene of side take-off is back to butylene isomerizing reactor 1 entrance, alkane alkene
Isomerization reaction by-product isolated by knockout tower 3--while lighter hydrocarbons, it is achieved that at the beginning of the concentration of isobutene. and alkane, alkene
Step separates.
Table 1 main technique operating parameter
Energy-saving and cost-reducing situation is shown in Table 2.
Table 2 energy consumption comparison
| Sequence number | Project | Original technique | Novel technique |
| 1 | Steam, t/h | 58 | 28 |
Remarks: the inlet amount of separation of alkane and olefin tower is 80t/h.
Use this energy saving technique technology, carry out butylene isomery coproduction MTBE, the plant investment of separation of alkane and olefin can be saved, save
All steam consumptions of separation of alkane and olefin, concrete saving expense can be according to the steam cost valency of olefin feedstocks concentration and plant running
Lattice calculate.According to device integral production situation, according to intermediate reboiler, to side line area above, carry out low-temperature level
Thermal source is supplied, and can reduce energy consumption greatly.
Above an example of the present invention is described in detail, but described content has been only the preferable enforcement of the present invention
Example, it is impossible to be considered the practical range for limiting the present invention.All impartial changes made according to the present patent application scope and improvement
Deng, within all should still belonging to the patent covering scope of the present invention.
Claims (4)
1. the energy-saving equipment of a butylene isomery coproduction MTBE, it is characterised in that include isomerizing reactor, compressor, separation of alkane and olefin
Tower, separation of alkane and olefin tower condenser, separation of alkane and olefin tower return tank, separation of alkane and olefin tower reboiler and MTBE unit, described isomerization reaction
Device outlet is connected with described separation of alkane and olefin tower charging aperture through compressor, described separation of alkane and olefin tower gas outlet and described separation of alkane and olefin
The air intake of tower condenser connects, and the liquid outlet of described separation of alkane and olefin tower condenser feeds with described separation of alkane and olefin tower return tank
Mouthful, described separation of alkane and olefin tower return tank discharging opening is connected with upper refluxing opening, the MTBE unit of described separation of alkane and olefin tower, is positioned at described
Liquid outlet at the bottom of separation of alkane and olefin tower tower is connected with fluid inlet, the lighter hydrocarbons extraction mouth of described separation of alkane and olefin tower reboiler, described alkane
The condensate outlet of alkene knockout tower reboiler is connected with the lower refluxing opening of described separation of alkane and olefin tower, and the liquid phase of described separation of alkane and olefin tower is adopted
Outlet is connected with described isomerizing reactor entrance.
The energy-saving equipment of a kind of butylene isomery coproduction MTBE the most as claimed in claim 1, it is characterised in that described separation of alkane and olefin
The number of plates of tower is 100 pieces, and the charging aperture of described separation of alkane and olefin tower is positioned at 35 pieces of Board positions, and the liquid phase of described separation of alkane and olefin tower is adopted
Outlet is positioned at 90 pieces of Board positions.
3. the energy-saving processing technique of a butylene isomery coproduction MTBE, it is characterised in that:
The material of isomerizing reactor outlet, is mainly composed of isobutene., n-butene, iso-butane, normal butane, and this strand of material is compressed
Machine enters separation of alkane and olefin tower；
Separation of alkane and olefin column overhead extraction material, is mainly composed of isobutene., iso-butane and a small amount of n-butene, normal butane, this stock
Material is through separation of alkane and olefin tower condenser and separation of alkane and olefin tower return tank, and a part is back to separation of alkane and olefin tower, and another part enters
MTBE unit, with methanol by after etherification reaction, without isobutene. in carbon four after ether, this strand of raw material is as alkylation feed；
The material of the liquid phase extraction mouth of separation of alkane and olefin tower, is mainly composed of normal butane, n-butene, and this strand of material parts is recycled to different
Structure reactor inlet, part extraction, after mixing with carbon after ether four, feed as alkyl plant；
Separation of alkane and olefin tower materials at bottom of tower, is mainly composed of lighter hydrocarbons, as product extraction.
The energy-saving processing technique of a kind of butylene isomery coproduction MTBE the most as claimed in claim 3, it is characterised in that separation of alkane and olefin
The reflux ratio scope of tower is 2.5 5.5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610451238.5A CN106008131A (en) | 2016-06-16 | 2016-06-16 | Energy-saving equipment and production process for producing MTBE with butane in heterogeneous co-production mode |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610451238.5A CN106008131A (en) | 2016-06-16 | 2016-06-16 | Energy-saving equipment and production process for producing MTBE with butane in heterogeneous co-production mode |
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| Publication Number | Publication Date |
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| CN106008131A true CN106008131A (en) | 2016-10-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610451238.5A Pending CN106008131A (en) | 2016-06-16 | 2016-06-16 | Energy-saving equipment and production process for producing MTBE with butane in heterogeneous co-production mode |
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| Country | Link |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101827804A (en) * | 2007-10-15 | 2010-09-08 | 巴斯夫欧洲公司 | Method for isomerizing olefins |
| CN104151122A (en) * | 2014-07-25 | 2014-11-19 | 东华工程科技股份有限公司 | Method for preparing isobutene by virtue of recycling C4 feedstock |
-
2016
- 2016-06-16 CN CN201610451238.5A patent/CN106008131A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101827804A (en) * | 2007-10-15 | 2010-09-08 | 巴斯夫欧洲公司 | Method for isomerizing olefins |
| CN104151122A (en) * | 2014-07-25 | 2014-11-19 | 东华工程科技股份有限公司 | Method for preparing isobutene by virtue of recycling C4 feedstock |
Non-Patent Citations (2)
| Title |
|---|
| 焦宁宁等，: ""正丁烯异构化生产异丁烯技术经济评价"", 《石油化工技术经济》 * |
| 黄英编著，: "《化工原理 下册》", 30 November 2006, 华东理工大学出版社，2006年11月第1版， * |
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Application publication date: 20161012 |