WO2019019034A1 - Dispositif de fractionnement de gaz - Google Patents

Dispositif de fractionnement de gaz Download PDF

Info

Publication number
WO2019019034A1
WO2019019034A1 PCT/CN2017/094415 CN2017094415W WO2019019034A1 WO 2019019034 A1 WO2019019034 A1 WO 2019019034A1 CN 2017094415 W CN2017094415 W CN 2017094415W WO 2019019034 A1 WO2019019034 A1 WO 2019019034A1
Authority
WO
WIPO (PCT)
Prior art keywords
tower
outlet
propylene
feed port
tee
Prior art date
Application number
PCT/CN2017/094415
Other languages
English (en)
Chinese (zh)
Inventor
张瑶
李艳兵
Original Assignee
深圳市宏事达能源科技有限公司
辽宁识微科技有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 深圳市宏事达能源科技有限公司, 辽宁识微科技有限公司 filed Critical 深圳市宏事达能源科技有限公司
Priority to PCT/CN2017/094415 priority Critical patent/WO2019019034A1/fr
Priority to CN201780005792.3A priority patent/CN108883343A/zh
Publication of WO2019019034A1 publication Critical patent/WO2019019034A1/fr

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series

Definitions

  • the invention relates to a gas fractionation device.
  • the petrochemical plant of Sinopec Zhongyuan Oilfield Company has a gas fractionation unit.
  • the feed of the gas fractionation unit comes from the liquefied gas produced by the catalytic cracking unit of the plant.
  • the non-condensable gas at the top of the deethanizer tower is added to the outlet of the catalytic cracking unit air compressor to add a pipeline, so that the non-condensable gas of the portion is returned to the catalytic cracking device.
  • 78.75% of the propylene content in the carbon tail gas at the top of the deethanizer tower can be reduced to 72.28%.
  • the volume fraction of propylene products in the top of the propylene tower can reach 99.6%, and the volume fraction of propane in the bottom can reach 95.0%. In 2013, it was modified to add an absorption tower.
  • the process is shown in Figure 1.
  • the volume fraction of the propylene product at the top of the propylene tower can reach 99.8%, which is the highest yield of domestic propylene products.
  • the device mixes the non-condensable gas at the top of the deethanizer into the diesel hydrogenated liquefied gas, and the propylene content in the diesel hydrogenated liquefied gas increases from 0% before the reform to 3.83% to 1.4 million tons.
  • the annual processing capacity 330 days a year, can recover 1,000 tons of propylene, the market price is about 5 million yuan, and the efficiency of consumption reduction is remarkable.
  • the present invention proposes a gas fractionation apparatus that solves the above drawbacks existing in the prior art.
  • a gas fractionation apparatus comprising a depropanizer, a deethanizer, a reboiler 1, a reboiler 2, and a propylene recovery tower, wherein the depropanizer is provided with a feed port 1.
  • the top discharge port of the column and the outlet port of the bottom of the column, the deethanizer tower is provided with a feed port 2, a top discharge port 2 and a bottom outlet port 2.
  • the propylene recovery tower is provided The feed port 3, the top inlet, the top outlet 3 and the bottom outlet 3, the inlet 3 is disposed at the bottom of the propylene recovery tower; the depropanizer is passed through the pipeline
  • the reboiler is connected in communication, and the deethanizer is connected to the reboiler through a pipeline;
  • the feed port of the depropanizer tower is connected to the raw material inlet through a pipeline, and the top discharge port of the tower is connected to the feed port through the pipeline; the top discharge port of the tower is connected to the feed port through the pipeline.
  • the bottom discharge port 3 is connected to the feed port through a pipe; the bottom discharge port of the bottom is connected to the first three-way pipe through a pipe, and the first three-way pipe has an outlet device, the first Another outlet of a tee is in communication with the top feed port.
  • the top discharge port of the column is connected to the condenser one, the reflux tank one and the second three-way pipe through a pipeline, and one of the outlets of the second three-way pipe is connected to the top of the depropanizer The other outlet of the second tee is in communication with the feed port.
  • the top outlet 2 is connected to the condenser 2, the reflux tank 2 and the third tee through a pipeline, and an outlet of the third tee is connected to the top of the deethanizer.
  • the other outlet of the third tee is in communication with the feed port three.
  • the other outlet of the first tee is in communication with the top feed port through a heat exchanger and a pump.
  • the other outlet of the first tee is in communication with the top inlet of the tower through a heat exchanger and a pump.
  • a feed tank is arranged between the feed port and the raw material inlet.
  • a fourth three-way pipe is disposed between the raw material inlet and the feed tank, the first end of the fourth three-way pipe is in communication with the raw material inlet, and the second end of the fourth three-way pipe Connected with the feed tank, the third end of the fourth tee is connected to the top discharge port.
  • the gas fractionation device of the invention adds a simple and easy-to-operate propylene recovery tower, and the C4 from the bottom of the depropanizer tower acts as an absorbent, so that it is no longer necessary to repurchase the absorbent, thereby saving cost.
  • C4 is fed as an absorbent from the top of the column, and C2 is not condensed from the bottom of the column.
  • the two materials are in reverse contact, which is beneficial for absorption.
  • the pressure of the propylene recovery tower is the same as the pressure of the top reflux tank of the depropanizer, which is favorable for returning to the depropanizer by the self-pressure of the absorbed C4.
  • Propylene is a high-priced and demanding product on the market, and the current situation is in short supply.
  • the invention further recovers the component of propylene in the liquefied gas by adding a propylene recovery tower, and then the propylene recovery tower tops
  • the yield of propylene products increased to 99.99%, and the propylene content in the non-condensable gas at the top of the deethanizer tower was reduced to 65.9%, which is the yield and recovery rate that cannot be achieved by the existing propylene recovery technology on the market.
  • the increased propylene recovery tower is not only simple to operate but also less expensive to invest.
  • Figure 1 is a flow chart of a prior art fractionation apparatus
  • FIG. 2 is a schematic view showing the structure of a gas fractionation apparatus according to the present invention.
  • a gas fractionation apparatus includes a depropanizer 10, a deethanizer 11, a reboiler-2, a reboiler 2, and a propylene recovery tower 12, and the depropanizer 10 is provided with a material outlet 1, a top discharge port 1 and a bottom outlet port 1.
  • the deethanizer column 11 is provided with a feed port 2, a top discharge port 2 and a bottom outlet port 2, and the propylene recovery
  • the tower 12 is provided with a feed port 3, an overhead feed port, a top discharge port 3, and a bottom discharge port 3.
  • the feed port 3 is disposed at the bottom of the propylene recovery column 12;
  • the propane column 10 is connected to the reboiler 2 through a pipe, and the deethanizer 11 is connected to the reboiler 2 through a pipe; the feed port of the depropanizer 10 is connected to the raw material inlet through a pipe.
  • the top outlet of the tower is connected to the inlet port through a pipeline; the outlet of the tower top is connected to the inlet port through the pipeline.
  • the bottom discharge port 3 is connected to the feed port through a pipe; the bottom discharge port is connected to the first three-way pipe through a pipe, and the first three-way pipe is an outlet device, the first Another outlet of the tee is in communication with the top feed port.
  • the top outlet of the tower is connected to the condenser 8 , the reflux tank 1 and the second tee through a pipeline, and one of the outlets of the second tee is connected to the top of the depropanizer 10 .
  • the other outlet of the second tee is in communication with the feed port.
  • the top outlet 2 is connected to the condenser 2, the reflux tank 2, and the third tee through a pipeline, and an outlet of the third tee is connected to the top of the deethanizer 11
  • the other outlet of the third tee is in communication with the feed port three.
  • the other outlet of the first tee is in communication with the top feed port through a heat exchanger 5 and a pump 6.
  • the other outlet of the first tee is in turn connected to the top feed port through the heat exchanger 5 and the pump 6.
  • a feed tank 7 is disposed between the feed port and the raw material inlet.
  • a fourth three-way pipe is disposed between the raw material inlet and the feed tank 7, the first end of the fourth three-way pipe is in communication with the raw material inlet, and the second end of the fourth three-way pipe is The tank is connected, and the third end of the fourth tee is connected to the top outlet of the tower.
  • the raw materials are mainly carbon di(C2H6), carbon tris(C3H6, C3H8) carbon tetra (C4H10, C4H8, C5H12, CCL2O (carbon oxychloride, a component in liquefied gas)).
  • the constituents of C. chinensis also include their isomers.
  • Feed tank 7 The raw material enters the tank before entering the tower equipment, and then flows into the tower through the pipeline;
  • the condenser reboilers are heat exchangers connected to the tower.
  • the depropanizer and deethanizer are functionally all rectification towers.
  • the general rectification towers are equipped with condensers and reboilers. of.
  • the propylene recovery tower is functionally an absorption tower.
  • the gas-liquid mixture at the top of the depropanizer column enters the deethanizer column. After a series of reactions, the light components are finally withdrawn from the top of the column. Because the bottom reboiler provides heat, a portion of the propylene is vaporized.
  • the main part of the tower is the non-condensable carbon, which contains some of our target products. (Now the average company chooses to directly mix the non-condensable gas into the civil liquefied gas and sell it directly as fuel. It will not be disposed of. There are very few companies that use this part of the non-condensable gas to be mixed into other workshops for use. In the previous report, there is a detailed description.)
  • the non-condensable gas coming out from the top of the deethanizer tower entrains part of the desired product propylene, so the present invention designs a propylene recovery tower for recovery.
  • the non-condensable gas enters from the bottom of the propylene recovery tower, the gas rises from the bottom, and the heavy component liquid from the bottom of the first tower depropanizer tower enters from the top of the propylene recovery tower, and the liquid flows from top to bottom, resulting in Reverse contact absorption.
  • the heavy component absorbs the propylene in the non-condensable gas, and the non-condensed gas hardly entrains the propylene, and then discharges the non-condensable gas from the top of the propylene recovery tower, which is the last destination after the non-condensable gas is absorbed.
  • the heavy component liquid that has absorbed propylene in the non-condensable gas is returned to the feed tank and mixed with the first raw material, so that more propylene enters the depropanizer column for a new round of rectification reaction to reach the propylene recovery tower. At that time, there will be more quality propylene.
  • the temperature is lowered to 35 ° C, and after the pressure of the pressure pump is increased to 2.6 MPa, one device is discharged, and the other channel is about 10 tons per hour into the top of the propylene recovery tower as an absorbent.
  • the propylene in the non-condensable gas C2 discharged from the top of the deethanizer is absorbed.
  • the non-condensable gas C2 in the top reflux tank of the deethanizer tower enters the bottom of the propylene recovery tower through the pipeline from the gas phase outlet of the reflux tank, and is in reverse contact with the C4 absorbent.
  • the propylene and propane in the non-condensable gas C2 are absorbed by the C4 absorbent.
  • the propylene recovery tower bottom can obtain a heavy component mixture containing a higher content of propylene, and the material is directly returned to the feed of the depropanizer, and mixed with the catalytic cracked product as a gas.
  • the sub-plant feeds into the depropanizer.
  • the high pressure and low temperature of the depropanizer tower is favorable for absorption, so the column pressure is set to 2.0 MPa, and the bottom of the propylene recovery tower is returned to the depropanizer column. Therefore, the propylene recovery tower pressure should be similar to that of the depropanizer reflux tank, and the propylene recovery tower.
  • the column pressure When the column pressure is set to 2.4 MPa, it can be self-pressurized without adding a pump. Low temperature and high pressure not only ensure the complete recovery of propylene and propane, but also reduce the emission loss of C4 fraction.
  • the content of propylene in the non-condensable gas at the top of the deethanizer column was 65.9%, and the purity of the propylene product distilled from the top of the propylene column was 99.99%.
  • Pressurized pump 6 The pressure of the material from the depropanizer is 18.5, and the pressure at the top of the propylene recovery tower is 2.4. It needs to be pressurized by the pump before entering the propylene recovery tower.
  • the pressure of the pump can be above 2.4, the pressure pump of 2.6 has more contact, and the actual situation may be floating, so the pump of 2.6 is selected.
  • a pressure difference of 0.5 is set at the bottom of each tower, and the pressure at the top of the tower is 0.5 MPa less than the pressure at the bottom of the tower.
  • the components in the tower are all components that are easily vaporized.
  • the temperature inside the tower is high, when the top of the tower is transported from the pipeline, it belongs to the gas and liquid.
  • the mixture after cooling by the overhead condenser, all became liquid and entered the reflux tank at the top. After turning into a liquid, it is beneficial to return to the reflux and transport to the next tower.
  • Second if there is gas, it may be partially evaporated and waste. The third is to recover heat. Therefore, one thing at the top of the material is to go to the top condenser and turn it into a liquid.
  • Condenser is a type of heat exchanger
  • the data and phase states listed in the table are cooled by the overhead condenser.
  • the propylene recovery tower can be used because the discharged material is in the gas phase, so no overhead condenser is added.
  • the liquefied gas is all in the liquid phase due to the pressurization, and the normal temperature and normal pressure are the gas phase.
  • Total feed The amount is 300,000 tons / year.
  • the gas fractionation unit When the propylene recovery column is not added, the gas fractionation unit directly discharges the mixed non-condensable gas containing C2H6 (0.09), C3H6 (0.3), and C3H8 (0.01) from the line B1. After the addition of the propylene recovery column, the propylene recovery column overhead D1 line discharges C2H6 (0.05) C3H6 (0.00006) and other components in the feed. It can be seen that the flow of propylene in the discharged non-condensable gas is significantly reduced.
  • the pipeline C3 contains C3H6 (0.3) and C3H8, C4H10, C4H8, C5H12, C5H10, CCL2O (total 10.01), it can be seen that for the propylene recovery tower, the feed in the A3 pipeline absorbs the B1 pipeline feed. The propylene, after absorption, is partially returned from the bottom line D3 with absorbed propylene and mixed with the raw material, so that about 0.3 million tons/year of propylene is recovered.
  • Pressurized pump 6 The pressure of the material from T-201 is 18.5, and the pressure at the top of the propylene recovery tower is 2.4. It needs to be pressurized by the pump before entering the propylene recovery tower.
  • the pressure of the pump can be above 2.4, the pressure pump of 2.6 has more contact, and the actual situation may be floating, so the pump of 2.6 is selected.
  • a pressure difference of 0.5 is set at the bottom of each tower, and the pressure at the top of the tower is 0.5 MPa less than the pressure at the bottom of the tower.
  • the components in the tower are components that are easily vaporized.
  • the top condensers 8, 9 are cooled, they all become liquid, and enter the top reflux tanks 1 and 2, respectively. After turning into a liquid, it is beneficial to return to the reflux and transport to the next tower.
  • Second if there is gas, it may be partially evaporated and waste. The third is to recover heat. Therefore, one thing at the top of the material is to go to the top condenser and turn it into a liquid.
  • Condenser is a type of heat exchanger
  • the data and phase states listed in the table are cooled by the overhead condenser.
  • the propylene recovery tower can be used because the discharged material is in the gas phase, so no overhead condenser is added.

Abstract

Un dispositif de fractionnement de gaz, comprenant une colonne d'élimination de propane (10), une colonne d'élimination d'éthane (2), un premier rebouilleur (2), un second rebouilleur (4) et une colonne de récupération de propylène (12). La colonne d'élimination de propane (10) est pourvue d'un premier orifice d'alimentation, d'un premier orifice de décharge de tête et d'un premier orifice de décharge inférieur. La colonne d'élimination d'éthane (11) est pourvue d'un second orifice d'alimentation, d'un second orifice de décharge de tête et d'un second orifice de décharge inférieur. La colonne de récupération de propylène (12) est pourvue d'un troisième orifice d'alimentation, d'un troisième orifice de décharge de tête et d'un troisième orifice de décharge inférieur.
PCT/CN2017/094415 2017-07-26 2017-07-26 Dispositif de fractionnement de gaz WO2019019034A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/CN2017/094415 WO2019019034A1 (fr) 2017-07-26 2017-07-26 Dispositif de fractionnement de gaz
CN201780005792.3A CN108883343A (zh) 2017-07-26 2017-07-26 一种气体分馏装置

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CN2017/094415 WO2019019034A1 (fr) 2017-07-26 2017-07-26 Dispositif de fractionnement de gaz

Publications (1)

Publication Number Publication Date
WO2019019034A1 true WO2019019034A1 (fr) 2019-01-31

Family

ID=64325574

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2017/094415 WO2019019034A1 (fr) 2017-07-26 2017-07-26 Dispositif de fractionnement de gaz

Country Status (2)

Country Link
CN (1) CN108883343A (fr)
WO (1) WO2019019034A1 (fr)

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1182443A (zh) * 1995-03-03 1998-05-20 先进提取技术有限公司 用于抑制反应副产物和从烯烃聚合过程中的废气物流中回收单体的吸收方法
US5890378A (en) * 1997-04-21 1999-04-06 Elcor Corporation Hydrocarbon gas processing
CN1683042A (zh) * 2005-02-08 2005-10-19 华南理工大学 双塔气体分馏装置及分馏方法
EP1637577A2 (fr) * 2004-07-02 2006-03-22 Kellogg Brown & Root, Inc. Basse presion récupération d'oléfines
CN102575898A (zh) * 2009-09-21 2012-07-11 奥特洛夫工程有限公司 碳氢化合物气体处理
CN204447370U (zh) * 2015-01-22 2015-07-08 中建安装工程有限公司 一种萃取精馏与闪蒸耦合分离丙烯和丙烷的装置
CN104784953A (zh) * 2015-03-26 2015-07-22 浙江大学 一种用于甲醇制丙烯的反应产物分离系统及其急冷系统
JP2016003215A (ja) * 2014-06-18 2016-01-12 住友化学株式会社 メチルアセチレンおよびプロパジエンの濃縮混合物の製造方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3833795A1 (de) * 1988-10-05 1990-04-12 Linde Ag Verfahren und vorrichtung zur aufarbeitung eines c(pfeil abwaerts)2(pfeil abwaerts)-stromes
US5372009A (en) * 1993-11-09 1994-12-13 Mobil Oil Corporation Cryogenic distillation
CN101445419B (zh) * 2007-11-27 2012-10-31 惠生工程（中国）有限公司 精馏与溶剂吸收相结合的含轻质气体低碳烃的分离方法
CN101367697B (zh) * 2008-10-15 2013-05-01 惠生工程（中国）有限公司 一种mto/mtp反应产物中轻烃产品的分离方法
CN101844961A (zh) * 2010-07-05 2010-09-29 茂名实华东成化工有限公司 高效回收脱乙烷塔顶乙烷气中丙烯的方法及其装置
CN104193575A (zh) * 2014-09-11 2014-12-10 中建安装工程有限公司 一种萃取精馏分离丙烷和丙烯的装置及方法

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1182443A (zh) * 1995-03-03 1998-05-20 先进提取技术有限公司 用于抑制反应副产物和从烯烃聚合过程中的废气物流中回收单体的吸收方法
US5890378A (en) * 1997-04-21 1999-04-06 Elcor Corporation Hydrocarbon gas processing
EP1637577A2 (fr) * 2004-07-02 2006-03-22 Kellogg Brown & Root, Inc. Basse presion récupération d'oléfines
CN1683042A (zh) * 2005-02-08 2005-10-19 华南理工大学 双塔气体分馏装置及分馏方法
CN102575898A (zh) * 2009-09-21 2012-07-11 奥特洛夫工程有限公司 碳氢化合物气体处理
JP2016003215A (ja) * 2014-06-18 2016-01-12 住友化学株式会社 メチルアセチレンおよびプロパジエンの濃縮混合物の製造方法
CN204447370U (zh) * 2015-01-22 2015-07-08 中建安装工程有限公司 一种萃取精馏与闪蒸耦合分离丙烯和丙烷的装置
CN104784953A (zh) * 2015-03-26 2015-07-22 浙江大学 一种用于甲醇制丙烯的反应产物分离系统及其急冷系统

Also Published As

Publication number Publication date
CN108883343A (zh) 2018-11-23

Similar Documents

Publication Publication Date Title
CN108558603B (zh) 一种三塔三效的粗甲醇精制工艺方法
CN209113783U (zh) 一种利用分壁塔分离高纯度异戊烷和正戊烷的分离系统
CN115317945B (zh) 烷基化反应产物两塔热耦合与热泵组合分离工艺及分离装置
CN103449950B (zh) 用贫液效应在脱甲烷过程中回收尾气中乙烯的方法及系统
CN112266799B (zh) 一种实现吸收稳定系统能耗降低的延迟焦化方法
CN102234541A (zh) 一种裂解汽油全馏分加氢节能方法和装置
CN100348286C (zh) 双塔气体分馏装置及分馏方法
CN102234540A (zh) 一种裂解汽油中心馏分加氢方法和装置
CN112358375B (zh) 两塔双热泵集成的1-丁烯精制节能工艺及装置
CN106495980A (zh) 基于前、后脱丙烷双塔流程的气分装置及方法
CN106588572B (zh) 一种低碳混合醇分离的三塔差压耦合精馏系统及方法
CN102641604B (zh) 一种多组分侧线热耦合精馏的工艺方法
WO2019019034A1 (fr) Dispositif de fractionnement de gaz
CN201686667U (zh) 一种裂解汽油全馏分加氢装置
CN107541235B (zh) 一种原油常压蒸馏塔塔顶油气的两段式冷凝、分离方法及分离系统
CN111187641B (zh) 一种催化裂化装置和加氢装置联合节能工艺流程
CN210346070U (zh) 一种甲醇制烯烃换热系统
CN101792679B (zh) 一种阶梯利用低温废水汽化丙烯脱聚合油塔进料的节能方法及装置
CN105087065A (zh) 一种裂解汽油中心馏分加氢装置及方法
CN210458013U (zh) 一种粗氢中乙烯的回收系统
CN202898270U (zh) 用贫液效应在脱甲烷过程中回收尾气中乙烯的系统
CN114307549B (zh) 一种降低炼油过程吸收稳定系统耗能的工艺
CN112321382B (zh) 具有热泵热集成的1-丁烯精制节能工艺及装置
CN115888155A (zh) 用于三组分混合物分离的精馏系统及精馏工艺
CN112760127B (zh) 一种油气分离及回收的装置和方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 17919044

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 17919044

Country of ref document: EP

Kind code of ref document: A1