CN103351271A - Device for recycling ethylene through solvent absorption method - Google Patents
Device for recycling ethylene through solvent absorption method Download PDFInfo
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- CN103351271A CN103351271A CN2013102856765A CN201310285676A CN103351271A CN 103351271 A CN103351271 A CN 103351271A CN 2013102856765 A CN2013102856765 A CN 2013102856765A CN 201310285676 A CN201310285676 A CN 201310285676A CN 103351271 A CN103351271 A CN 103351271A
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- ethene
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The invention relates to a petrochemical plant, in particular to a device for recycling ethylene through a solvent absorption method. The device is characterized in that feed gas enters from the bottom of an absorption tower; a mixed butane poor absorbent is added from the top of the absorption tower and is reversely contacted with hydrogen gas, methane gas, carbon monoxide gas and ethylene gas coming from the bottom of the absorption tower; most of the ethylene is absorbed by a solvent to form a rich absorbent; the rich absorbent enters the tower kettle of the absorption tower; under own pressure, the rich absorbent and the poor absorbent are subjected to cold recovery in a heat exchanger and then enter in the tower top of a regenerating column; the gas, of which the ethylene is recovered at the tower top of the absorption tower, is discharged as a fuel gas. The device has the advantages that overhigh pressure and extremely low temperature are not necessary for absorption, the recovery efficiency of ethylene can reach more than 90%; the relative volatility of the butane absorbent is lower than the volatility of a propane hydrocarbon component, the loss of the butane absorbent in the process is low and great supplementation of the butane absorbent is not needed; appropriate regeneration pressure is selected so as to facilitate further recovery processing of ethylene; a lower regeneration temperature can be controlled so that the waste low-temperature heat of the device is used in the regeneration process to reduce energy consumption.
Description
Technical field:
The present invention relates to a kind of petrochemical equipment, more particularly, relate to a kind of device that reclaims ethene.
Background technology:
In the conventional low-carbon alkene production technique, for with fuel gas composition effective separations such as ethene and methane and hydrogen, generally all adopt high pressure, low temperature separating process, namely under higher working pressure and lower temperature, at first with ethene liquefaction, recycling rectification process realization ethene separates with other composition.The ice maker of this arts demand setting take ethene as refrigeration agent, the working pressure that is higher than 3.0MPaG be lower than-100 ℃ of temperature under realize separating of ethene.
In preparing propylene from methanol (MTP) production technique, the output of ethene only account for propone output less than 5%, if adopt conventional separating technology then need to arrange the ethylene refrigeration ice maker, simultaneously will be to the further pressure treatment of light hydrocarbon gas.Like this, sepn process needs larger facility investment and higher energy consumption.
Summary of the invention:
The object of the invention is to overcome the deficiency of prior art, the device of the recovery ethene in a kind of preparing propylene from methanol device is provided.
The present invention is directed to the production low-carbon alkene technological processs such as preparing propylene from methanol (MTP), adopt solvent absorption process, low-concentration ethane contained in the light hydrocarbon gas such as methane is carried out effective separation; Used lyosorption is the hydrocarbon mixture of process unit by-product.
In production low-carbon alkene techniques such as preparing propylene from methanol (MTP), develop the technique that a cover solvent absorption reclaims the low-concentration ethane in separating hydrogen gas, methane and the carbon monoxide.Utilize this Technology, can be than low operating pressure, be usually less than 2.4MPaG, under the higher refrigerant temperature condition, high efficiency separation reclaims ethene, reduce ethene with the loss of carrying of fuel gas, and reduced investment, energy consumption low, be widely used, can be successfully applied to the fields such as preparing propylene from methanol (MTP), methanol-to-olefins (MTO) and ethylene unit.
The component of the mixed c 4 of adopting process device by-product of the present invention is as absorption agent, this absorption agent is absorbing the cat head adding, under the working pressure peace treaty-35 ℃ temperature condition of 1.8～2.4MPaG, contact with gas material is reverse from the hydrogen at the bottom of the tower, methane, carbon monoxide and ethene etc., ethene is high because of the solubleness in lyosorption, and by solvent absorbing, ethene absorbs in the liquid phase, at the bottom of tower, be delivered to desorption tower, discharge the ethene composition of recovery through regenerative process, the solvent after the regeneration can be recycled.And removing the gas such as hydrogen, methane, carbon monoxide of ethene, the gas that then acts as a fuel is discharged by the top, absorption tower.
Solvent absorption reclaims the device of ethene, it is characterized in that, is provided with absorption tower, regenerator column, interchanger, force (forcing) pump, water cooler, moisture eliminator, reboiler equipment; The unstripped gas that contains ethene from the demethanizing system, entered by the bottom, absorption tower, the poor absorption agent of mixed c 4 is added by the top, absorption tower, be filled with the filler that promotes gas-to-liquid contact in the absorption tower, the absorbing tower pressure on top surface is 1.8～2.4MPaG, tower top temperature is-30～-45 ℃, column bottom temperature-11 ℃, with from the hydrogen at the bottom of the tower, methane, carbon monoxide, the reverse contact of ethylene gas, most of ethene is formed rich absorbent by solvent absorbing, and rich absorbent enters the absorption tower tower reactor, own pressure and poor absorption agent reclaim cold in interchanger after, enter the regenerator column cat head; The absorption tower cat head reclaims gas behind the ethene gas that acts as a fuel and discharges; The top pressure of regenerator column is 1.1MPaG, and tower top temperature is 4 ℃, and the regenerator column bottom temp is 67 ℃, and the regenerator column bottom is provided with reboiler; Rich absorbent is deviate from ethene because of hot stripping effect by regeneration overhead, and obtains regeneration, and regenerator column top ethene enters the further refine and reclaim of subsequent disposal system; Poor absorption agent at the bottom of the regenerator column, through after the force (forcing) pump pressurization, at first in interchanger with the rich absorbent heat exchange, further be cooled to-35 ℃ through water cooler with-41 ℃ propylene refrigerant again, return the top on absorption tower; The absorption agent that loses in the process, the mixed c 4 hydro carbons by from distillation system adds in the system after drying.
Certainly, used lyosorption also can be selected from equally by hydrocarbon components such as the carbon three of device by-product or carbon five, but the volatility of assimilated efficiency, solvent of comprehensive solvent own, the required factors such as temperature, pressure condition of regeneration, the utilization of mixed c 4 is fit to beyond doubt the most.
The invention has the advantages that: absorption need not too high pressure and extremely low temperature, and the organic efficiency of ethene can reach more than 90%; Carbon four absorption agent relative volatilities are lower than carbon three hydrocarbon component volatilization degree, and loss amount is little in the process, and absorption agent need not a large amount of replenishing; Select suitable regeneration pressure, be conducive to the further recycling of ethene, can control lower regeneration temperature, the heat of useless low temperature of device is used in regenerative process, reduce energy consumption.
Description of drawings
Fig. 1 is simplification of flowsheet figure of the present invention.
Absorption tower 1, regenerator column 2, interchanger 3, force (forcing) pump 4, water cooler 5, moisture eliminator 6, reboiler 7 are arranged among the figure.
Embodiment
Below in conjunction with the drawings and specific embodiments, further detailed description is made in invention.
As shown in the figure, the unstripped gas that contains 60% ethene from the demethanizing system, entered by 1 bottom, absorption tower, the poor absorption agent of mixed c 4 is added by absorption tower 1 napex, be filled with the filler that promotes gas-to-liquid contact in the absorption tower 1, absorption tower 1 tower top pressure is 1.8～2.4MPaG, tower top temperature is-30～-45 ℃, column bottom temperature-11 ℃, with from the hydrogen at the bottom of the tower, methane, carbon monoxide, the reverse contact of ethylene gas, most of ethene is by solvent absorbing, form rich absorbent, rich absorbent enters absorption tower 1 tower reactor, and own pressure and poor absorption agent are behind interchanger 3 interior recovery colds, enter regenerator column 2 tops, the gas that acts as a fuel of the gas behind the 1 recovered overhead ethene of absorption tower is discharged by absorption tower 1 cat head; The top pressure of regenerator column 2 is 1.1MPaG, and tower top temperature is 4 ℃, and regenerator column 2 bottom temps are 67 ℃, and regenerator column 2 bottoms are provided with reboiler 7; Rich absorbent is deviate from ethene because of hot stripping effect by regenerator column 2 tops and is obtained regeneration, and regenerator column 2 top ethene enter the further refine and reclaim of subsequent disposal system.The poor absorption agent in 2 ends of regenerator column, after force (forcing) pump 4 pressurization, at first interchanger 3 in and the rich absorbent heat exchange, the propylene refrigerant through water cooler 5 usefulness-41 ℃ further is cooled to-35 ℃ again, returns the top on absorption tower 1; The absorption agent that loses in the process by the mixed c 4 hydro carbons from distillation system, adds in the system after drying device 6 dryings.
The unstripped gas of the ethene of described X%, its percentage ratio are percent by volume, and described XMPaG is gauge pressure.
Claims (1)
1. a solvent absorption reclaims the device of ethene, it is characterized in that, be provided with absorption tower (1), regenerator column (2), interchanger (3), force (forcing) pump (4), water cooler (5), moisture eliminator (6), reboiler (7) equipment, the unstripped gas that contains ethene from the demethanizing system, entered by absorption tower (1) bottom, the poor absorption agent of mixed c 4 is added by top, absorption tower (1), be filled with the filler that promotes gas-to-liquid contact in the absorption tower (1), absorption tower (1) tower top pressure is 1.8～2.4MPaG, tower top temperature is-30～-45 ℃, column bottom temperature-11 ℃, with from the hydrogen at the bottom of the tower, methane, carbon monoxide, the reverse contact of ethylene gas, most of ethene is by solvent absorbing, form rich absorbent, rich absorbent enters absorption tower (1) tower reactor, own pressure and poor absorption agent reclaim cold in interchanger (3) after, enter regenerator column (2) cat head, the gas that acts as a fuel of the gas behind the recovered overhead ethene of absorption tower (1) is discharged; The top pressure of regenerator column (2) is 1.1MPaG, and tower top temperature is 4 ℃, and regenerator column (2) bottom temp is 67 ℃, and regenerator column (2) bottom is provided with reboiler (7); Rich absorbent is because of hot stripping effect, deviate from ethene and obtain regeneration by regenerator column (2) top, regenerator column (2) top ethene enters the further refine and reclaim of subsequent disposal system, the poor absorption agent in regenerator column (2) end, after force (forcing) pump (4) pressurization, at first in interchanger (3) with the rich absorbent heat exchange, further be cooled to-35 ℃ through water cooler (5) with-41 ℃ propylene refrigerant again, return the top of absorption tower (1); The absorption agent that loses in the process by the mixed c 4 hydro carbons from distillation system, adds in the system after drying device (6) drying.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013102856765A CN103351271A (en) | 2013-06-28 | 2013-06-28 | Device for recycling ethylene through solvent absorption method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013102856765A CN103351271A (en) | 2013-06-28 | 2013-06-28 | Device for recycling ethylene through solvent absorption method |
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| CN103351271A true CN103351271A (en) | 2013-10-16 |
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| CN2013102856765A Pending CN103351271A (en) | 2013-06-28 | 2013-06-28 | Device for recycling ethylene through solvent absorption method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678639A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of separation method and device of Catalyst for Oxidative Coupling of Methane reaction gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4160810A (en) * | 1978-03-07 | 1979-07-10 | Benfield Corporation | Removal of acid gases from hot gas mixtures |
| CN101139237A (en) * | 2006-09-08 | 2008-03-12 | 北京化工大学 | Separating process for olefin-containing gas |
| CN101659590A (en) * | 2009-09-15 | 2010-03-03 | 中国石油化工集团公司 | Refining method of raw material gas containing ethene in process of preparing ethylbenzene from ethene |
| CN102267850A (en) * | 2010-06-02 | 2011-12-07 | 中国石油化工集团公司 | Method for separating light olefins gas |
-
2013
- 2013-06-28 CN CN2013102856765A patent/CN103351271A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4160810A (en) * | 1978-03-07 | 1979-07-10 | Benfield Corporation | Removal of acid gases from hot gas mixtures |
| CN101139237A (en) * | 2006-09-08 | 2008-03-12 | 北京化工大学 | Separating process for olefin-containing gas |
| CN101659590A (en) * | 2009-09-15 | 2010-03-03 | 中国石油化工集团公司 | Refining method of raw material gas containing ethene in process of preparing ethylbenzene from ethene |
| CN102267850A (en) * | 2010-06-02 | 2011-12-07 | 中国石油化工集团公司 | Method for separating light olefins gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678639A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of separation method and device of Catalyst for Oxidative Coupling of Methane reaction gas |
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Application publication date: 20131016 |