CN108147941A - Liquefied gas component separation of alkane and olefin system and separation method - Google Patents
Liquefied gas component separation of alkane and olefin system and separation method Download PDFInfo
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- CN108147941A CN108147941A CN201711403921.2A CN201711403921A CN108147941A CN 108147941 A CN108147941 A CN 108147941A CN 201711403921 A CN201711403921 A CN 201711403921A CN 108147941 A CN108147941 A CN 108147941A
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- tower
- alkane
- olefin
- liquefied gas
- separation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of liquefied gas component separation of alkane and olefin system and separation methods, belong to chemical products separating and purifying technology field.A kind of liquefied gas component separation of alkane and olefin system of the present invention includes separation of alkane and olefin tower etc.；Liquefied gas component separation of alkane and olefin method of the present invention is implemented by above-mentioned liquefied gas component separation of alkane and olefin system.Liquefied gas component separation of alkane and olefin system of the present invention and separation method so that filler column overhead be alkane component olefin-containing 13.9%, alkane 86.4%；Tower reactor is olefin component, concentration of olefin concentrate to 65.5%, when effectively raising the concentration of alkene, then carrying out alkene utilization, the energy consumption that alkene will be substantially reduced utilizes.Liquefied gas component separation of alkane and olefin system of the present invention has the technique effects such as energy-saving, raising environmental protection with separation method.
Description
Technical field
The present invention relates to a kind of piece-rate system and separation method, more particularly to a kind of liquefied gas component separation of alkane and olefin system with
Separation method belongs to chemical products separating and purifying technology field.
Background technology
Olefin component in liquefied gas is used for the numerous areas of chemical industry synthesis, but often effective concentration of olefin is very low, causes
When utilizing alkene, directly liquefied gas is fed, product energy consumption can be made very big, processing cost increases.If before alkene utilization, first
Material alkane separation in liquefied gas is come out, the concentration of effective alkene is improved, then carry out alkene utilization, alkene will be substantially reduced
The energy consumption utilized.
Invention content
The technical problems to be solved by the invention are that the defect of the prior art is overcome to provide a kind of liquefied gas component alkane alkene point
From system and separation method, alkane is detached for providing, improves the concentration of effective alkene.
Problem to be solved by this invention is realized by following technical scheme：
First, the present invention provides a kind of liquefied gas component separation of alkane and olefin system, which includes separation of alkane and olefin tower；The alkane alkene
Knockout tower includes packed tower with being located at the tower reactor below packed tower and being attached thereto；The tower top of the packed tower by pipeline with it is cold
Condenser connects, and condenser is connect by pipeline with return channel；Return channel is connect by pipeline with reflux pump, and reflux pump passes through pipeline
It is connect with the tower top of packed tower；Extraction pipeline is provided on pipeline between the reflux pump and the tower top of packed tower；It is described
Tower reactor bottom is connect by pipeline with Steam reboiler, and Steam reboiler is connect by pipeline with tower reactor side；The packed tower
It is disposed with the first packing section, the second packing section, third packing section, the 4th packing section, the 5th packing section from bottom to top, every section
Packed height 6500mm, filler are stainless steel ripple gauze structured packing；It is respectively arranged in the first packing section, the second packing section
Lower feed inlet, enterprising material mouth；The lower feed inlet, enterprising material mouth are connect with raw material input channel；The tower reactor bottom passes through pipe
Road and extraction pump connection.
The further present invention provides a kind of liquefied gas component separation of alkane and olefin method, by above-mentioned liquefied gas component alkane alkene point
Implement from system.
Specifically, the present invention provides a kind of liquefied gas component separation of alkane and olefin method, include the following steps：
(I) packed tower absolute pressure of top of the tower 750kpa, 53.4 DEG C of temperature are kept, alkane component is high in liquefied gas raw material components
When 62%, with lower feed inlet；During less than 62%, with feed inlet；
(II) tower reactor bottom absolute pressure 751kpa, 57.6 DEG C of temperature are kept, tower reactor provides heat source through Steam reboiler, will
The material of tower reactor bottom is heated, and Steam reboiler is heated by 1.0MPa steam, maintains the reflux for 53.4 DEG C of temperature；
(III) the condensed device of packed tower tower top material is condensed to liquid, and into return channel, condenser takes heat with recirculated water；
(IV) material in return channel returns stream through a reflux pump part to filler column overhead, and a part is by producing pipeline
Extraction, the mass ratio of reflux and extraction are controlled 4.5：1；
(V) kettle material is through extraction pump extraction；
(VI) detach after material, filler column overhead be alkane component olefin-containing 13.9%, alkane 85.6%；Tower reactor is alkene
The hydrocarbon component, concentration of olefin concentrate to 65.5%.
The present invention has the advantage that for existing：
Liquefied gas component separation of alkane and olefin system of the present invention and separation method so that filler column overhead contains for alkane component
Alkene 13.9%, alkane 86.0%；Tower reactor is olefin component, and concentration of olefin concentrate to 65.5% effectively raises alkene
Concentration, then when carrying out alkene utilization, the energy consumption for alkene will be substantially reduced utilizing.Liquefied gas component separation of alkane and olefin system of the present invention
System has the technique effects such as energy-saving, raising environmental protection with separation method.
Description of the drawings
Fig. 1 is the schematic diagram of liquefied gas component separation of alkane and olefin system of the present invention；
Reference sign：Packed tower 1, tower reactor 2, condenser 3, Steam reboiler 4, return channel 5, reflux pump 6, extraction pump
(7), enterprising material mouth 8, lower feed inlet 9, the first packing section A, the second packing section B, third packing section C, the 4th packing section D, the 5th
Packing section E.
Specific embodiment
The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.
Liquefied gas component separation of alkane and olefin system of the present invention, the system include separation of alkane and olefin tower；The separation of alkane and olefin tower packet
Include packed tower 1 and the tower reactor 2 for being located at 1 lower section of packed tower and being attached thereto；The tower top of the packed tower 1 passes through pipeline and condenser
3 connections, condenser 3 are connect by pipeline with return channel 5；Return channel 5 is connect by pipeline with reflux pump 6, and reflux pump 6 passes through pipe
Road is connect with the tower top of packed tower 1；Extraction pipeline is provided on pipeline between the reflux pump 6 and the tower top of packed tower 1；
2 bottom of tower reactor is connect by pipeline with Steam reboiler 4, and Steam reboiler 4 is connect by pipeline with 2 side of tower reactor；Institute
It states packed tower 1 and is disposed with the first packing section A, the second packing section B, third packing section C, the 4th packing section D, from bottom to top
Five packing section E, every section of packed height 6500mm, filler is stainless steel ripple gauze structured packing；In the first packing section A, second
Packing section B is respectively arranged with lower feed inlet 9, enterprising material mouth 8；The lower feed inlet 9, enterprising material mouth 8 and raw material input channel connect
It connects；2 bottom of tower reactor is connect by pipeline with extraction pump 7.
With reference to liquefied gas component separation of alkane and olefin system, the separation of liquefied gas raw material is carried out, liquefied gas raw material composition is shown in
Table 1.
1. liquefied gas raw material forms
As shown in Table 1, raw material olefin total content is 37.62%, and alkane total content is 62.32%.
(I) packed tower 1 absolute pressure of top of the tower 750kpa, 53.4 DEG C of temperature are kept, alkane component in liquefied gas raw material components
During higher than 62%, with lower feed inlet 9；
(II) 2 bottom absolute pressure 751kpa of tower reactor, 57.6 DEG C of temperature are kept, tower reactor (2) provides heat through Steam reboiler 4
The material of 2 bottom of tower reactor is heated in source, and Steam reboiler 4 is heated by 1.0MPa steam, maintains the reflux for temperature 53.4
℃；
(III) the condensed device 3 of 1 tower top material of packed tower is condensed to liquid, and into return channel 5, condenser 3 is taken with recirculated water
Heat；
(IV) material in return channel 5 returns stream through 6 part of reflux pump to 1 tower top of packed tower, and a part passes through extraction
Pipeline produces, and the mass ratio of reflux and extraction is controlled 4.5：1；
(V) kettle material is through 7 extraction of extraction pump；
(VI) detach after material, 1 tower top of packed tower be alkane component olefin-containing 13.96%, alkane 86.04%；Tower reactor 2
For olefin component, it is shown in Table 2.
2. the product form after separation of alkane and olefin
| Component | Mass fraction % |
| Iso-butane | 13.739 |
| Normal butane | 20.12 |
| N-butene | 18.27 |
| Anti- butylene | 16.8 |
| Pentane | 0.584 |
| Isobutene | 17.78 |
| Maleic | 12.574 |
| 1,3- butadiene | 0.134 |
| It amounts to | 100.001 |
As shown in Table 2, theatotal olefinsacontent is promoted to 65.558%, and alkane total content is reduced to 34.442%.
The explanation of above example is only intended to help to understand the present invention, enable professional and technical personnel in the field realize or
Using the present invention, it is not intended to restrict the invention, it is all within the spirits and principles of the present invention, any modification for being made, equivalent
Replace, improve etc., it should all be included in the protection scope of the present invention.
Claims (3)
1. a kind of liquefied gas component separation of alkane and olefin system, which is characterized in that the system includes separation of alkane and olefin tower；The separation of alkane and olefin tower
Including packed tower (1) with being located at the tower reactor (2) below packed tower (1) and being attached thereto；The tower top of the packed tower (1) passes through pipe
Road is connect with condenser (3), and condenser (3) is connect by pipeline with return channel (5)；Return channel (5) passes through pipeline and reflux pump
(6) it connects, reflux pump (6) is connect by pipeline with the tower top of packed tower (1)；In the reflux pump (6) and the tower of packed tower (1)
Extraction pipeline is provided on pipeline between top；Tower reactor (2) bottom is connect by pipeline with Steam reboiler (4), steam
Reboiler (4) is connect by pipeline with tower reactor (2) side；The packed tower (1) is disposed with the first packing section from bottom to top
(A), the second packing section (B), third packing section (C), the 4th packing section (D), the 5th packing section (E), every section of packed height
6500mm, filler are stainless steel ripple gauze structured packing；In the case where the first packing section (A), the second packing section (B) are respectively arranged with
Feed inlet (9), enterprising material mouth (8)；The lower feed inlet (9), enterprising material mouth (8) are connect with raw material input channel；The tower reactor
(2) bottom is connect by pipeline with extraction pump (7).
A kind of 2. liquefied gas component separation of alkane and olefin method, which is characterized in that it is by liquefied gas component alkane alkene described in claim 1
Piece-rate system is implemented.
3. liquefied gas component separation of alkane and olefin method according to claim 2, which is characterized in that include the following steps：
(I) packed tower (1) absolute pressure of top of the tower 750kpa, 53.4 DEG C of temperature are kept, alkane component is high in liquefied gas raw material components
When 62%, with lower feed inlet (9)；During less than 62%, with feed inlet (8)；
(II) tower reactor (2) bottom absolute pressure 751kpa, 57.6 DEG C of temperature are kept, tower reactor (2) provides heat through Steam reboiler (4)
The material of tower reactor (2) bottom is heated in source, and Steam reboiler (4) is heated by 1.0MPa steam, maintains the reflux for temperature
53.4℃；
(III) the condensed device of packed tower (1) tower top material (3) condensation is to liquid, into return channel (5), condenser (3) cycle
Water takes heat；
(IV) material in return channel (5) returns stream through reflux pump (6) part to packed tower (1) tower top, and a part is by adopting
Go out pipeline extraction, the mass ratio of reflux and extraction is controlled 4.5：1；
(V) kettle material is through extraction pump (7) extraction；
(VI) detach after material, packed tower (1) tower top be alkane component olefin-containing 13.9%, alkane 86.0%；Tower reactor (2) is
Olefin component, concentration of olefin concentrate to 65.5%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711403921.2A CN108147941B (en) | 2017-12-22 | 2017-12-22 | Liquefied gas component alkane and alkene separation system and separation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711403921.2A CN108147941B (en) | 2017-12-22 | 2017-12-22 | Liquefied gas component alkane and alkene separation system and separation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108147941A true CN108147941A (en) | 2018-06-12 |
| CN108147941B CN108147941B (en) | 2020-09-08 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711403921.2A Active CN108147941B (en) | 2017-12-22 | 2017-12-22 | Liquefied gas component alkane and alkene separation system and separation method |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4608069A (en) * | 1984-03-12 | 1986-08-26 | Linde Aktiengesellschaft | Separation of higher boiling impurities from liquefied gases |
| CN101844960A (en) * | 2009-03-23 | 2010-09-29 | 上海傲佳能源科技有限公司 | Method for producting propylene by catalytic pyrolysis of liquefied gas |
| CN101935265A (en) * | 2009-06-29 | 2011-01-05 | 上海傲佳能源科技有限公司 | Liquefied gas catalytic pyrolysis process |
| CN102757297A (en) * | 2011-04-27 | 2012-10-31 | 中国石油化工股份有限公司 | Method for producing efficient ethylene pyrolysis feedstock by liquefied gas |
| CN104689589A (en) * | 2015-02-13 | 2015-06-10 | 杭州杭氧填料有限公司 | Vortex-line self-homogenizing regulation packing tower |
| CN204543610U (en) * | 2015-02-13 | 2015-08-12 | 杭州杭氧填料有限公司 | Vortex filament shape is from uniform regular packed tower |
| CN106495980A (en) * | 2016-09-29 | 2017-03-15 | 大连理工大学 | Gas separation unit and method based on forward and backward depropanization double-column process |
| CN107285984A (en) * | 2016-04-11 | 2017-10-24 | 中国石化工程建设有限公司 | The combination process that a kind of gas fractionation unit is expanded production and saved |
-
2017
- 2017-12-22 CN CN201711403921.2A patent/CN108147941B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4608069A (en) * | 1984-03-12 | 1986-08-26 | Linde Aktiengesellschaft | Separation of higher boiling impurities from liquefied gases |
| CN101844960A (en) * | 2009-03-23 | 2010-09-29 | 上海傲佳能源科技有限公司 | Method for producting propylene by catalytic pyrolysis of liquefied gas |
| CN101935265A (en) * | 2009-06-29 | 2011-01-05 | 上海傲佳能源科技有限公司 | Liquefied gas catalytic pyrolysis process |
| CN102757297A (en) * | 2011-04-27 | 2012-10-31 | 中国石油化工股份有限公司 | Method for producing efficient ethylene pyrolysis feedstock by liquefied gas |
| CN104689589A (en) * | 2015-02-13 | 2015-06-10 | 杭州杭氧填料有限公司 | Vortex-line self-homogenizing regulation packing tower |
| CN204543610U (en) * | 2015-02-13 | 2015-08-12 | 杭州杭氧填料有限公司 | Vortex filament shape is from uniform regular packed tower |
| CN107285984A (en) * | 2016-04-11 | 2017-10-24 | 中国石化工程建设有限公司 | The combination process that a kind of gas fractionation unit is expanded production and saved |
| CN106495980A (en) * | 2016-09-29 | 2017-03-15 | 大连理工大学 | Gas separation unit and method based on forward and backward depropanization double-column process |
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| CN108147941B (en) | 2020-09-08 |
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