WO2022000735A1 - 一种低温甲醇洗洗涤富液co 2解吸装置及方法 - Google Patents

一种低温甲醇洗洗涤富液co 2解吸装置及方法 Download PDF

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WO2022000735A1
WO2022000735A1 PCT/CN2020/110344 CN2020110344W WO2022000735A1 WO 2022000735 A1 WO2022000735 A1 WO 2022000735A1 CN 2020110344 W CN2020110344 W CN 2020110344W WO 2022000735 A1 WO2022000735 A1 WO 2022000735A1
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section
washing
rich liquid
methanol
desorption
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PCT/CN2020/110344
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English (en)
French (fr)
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张述伟
管凤宝
赵晋
李燕
梁锋
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大连佳纯气体净化技术开发有限公司
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Priority claimed from CN202021254803.7U external-priority patent/CN212395910U/zh
Priority claimed from CN202010621535.6A external-priority patent/CN113856231A/zh
Application filed by 大连佳纯气体净化技术开发有限公司 filed Critical 大连佳纯气体净化技术开发有限公司
Publication of WO2022000735A1 publication Critical patent/WO2022000735A1/zh

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    • 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
    • B01D3/06—Flash distillation

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  • the present application relates to a low-temperature methanol washing and washing rich liquid CO 2 desorption device and method.
  • the low-temperature methanol washing process is widely used in the production of synthetic ammonia, city gas, industrial hydrogen, synthetic methanol or some other carbon chemicals from coal (petroleum coke) or residual oil.
  • the process is to absorb the acid gas in the mixed gas with methanol, usually CO 2 or CO 2 and H 2 S, and then separate the methanol from the acid gas through decompression desorption, stripping and heating to achieve the purpose of separation and recovery.
  • the absorption capacity of methanol to acid gas decreases with the increase of temperature. In order to improve the absorption capacity of methanol to acid gas and reduce the amount of solvent circulation, it is necessary to maintain the methanol washing device to operate at low temperature.
  • the flow of the methanol-rich liquid is driven by the pressure difference between the CO 2 desorption tower and the H 2 S concentration tower, but usually the pressure difference between the two towers is very small, and there is still a gap between the connecting nozzles of the two towers.
  • a certain potential difference the nozzle of the CO 2 desorption tower is low and the nozzle of the H 2 S concentration tower is high
  • the pipeline resistance is too large, the flow of the methanol-rich liquid will be sluggish, and the methanol circulation process cannot be carried out normally.
  • the present application provides a low-temperature methanol washing and washing rich liquid CO 2 desorption device and method, by adding a D-1 section at the bottom of the CO 2 desorption tower, and using the D-1 section to flash the rich methanol, At the same time, the height of the A-1, B-1, C-1 sections of the original CO 2 desorption tower is increased, and the position difference between the nozzles corresponding to the H 2 S concentration tower is reduced, so as to ensure the smooth flow of methanol-rich towers in the two towers.
  • the present application proposes a low-temperature methanol washing and washing rich liquid CO 2 desorption device, including a CO 2 desorption tower and an H 2 S concentration tower;
  • the CO 2 desorption tower is provided with C-1 section and D-1 section from top to bottom;
  • the D-1 section is respectively connected with the H 2 S concentration tower and the C-1 section, and is used for continuing the flash treatment of the flashed sulfur-containing methanol-rich liquid in the H 2 S concentration tower.
  • the liquid outlet arranged in the middle of the H 2 S concentration tower is communicated with the liquid inlet of the D-1 section of the CO 2 desorption tower, so that the sulfur-containing methanol-rich liquid after gas stripping in the H 2 S concentration tower enters.
  • section D-1 flash treatment I is performed;
  • the top section is provided in communication with the gas outlet section I C-1, for processing to give after flash I of CO 2 into the flash vapor segment C-1;
  • the bottom of the D-1 section is provided with a liquid outlet communicating with the C-1 section, which is used to pass the remaining sulfur-containing methanol-rich liquid obtained through the flash distillation treatment I into the C-1 section for the flash distillation treatment II.
  • the CO 2 desorption tower also includes A-1 section and B-1 section, A-1 section is located above B-1 section, B-1 section is located above C-1 section;
  • the lower part of the A-1 section is connected with the upper part of the A-2 section through a pipeline;
  • the lower part of the B-1 section is connected with the middle part of the B-2 section through a pipeline; the lower part of the B-2 section is connected with the upper part of the C-1 section through a pipeline;
  • the lower part of the C-1 section is connected with the upper part of the C-2 section through a pipeline;
  • the upper part of the A-1 section is provided with a liquid inlet I; the middle of the B-1 section is provided with a liquid inlet II;
  • the top of the C-1 section and the top of the B-1 section are provided with a gas outlet II connected to the B-1 section and the A-1 section respectively;
  • section A-1 The top of section A-1, the top of section A-2 and the upper part of section B-2 are all provided with air outlet III;
  • the lower part of the A-2 section is provided with a liquid outlet I;
  • the lower part of the C-2 section is provided with a stripping gas inlet, and the bottom of the C-2 section is provided with a liquid outlet II;
  • the lower part of the A-1 section is connected with the upper part of the B-1 section through a pipeline;
  • the bottom of the A-2 section is connected with the upper part of the B-2 section through a pipeline.
  • the height of section D-1 is 8-10 meters.
  • a transfer pump and a heat exchanger are arranged on the pipeline connecting the H 2 S concentration tower and the D-1 section.
  • a transfer pump and a heat exchanger are arranged on the pipeline connecting the D-1 section and the C-1 section.
  • Rectisol washing rich liquid CO 2 desorption process comprising the steps of:
  • the remaining sulfur-containing methanol-rich liquid is passed into the C-1 section of the CO 2 desorption tower, so that the remaining sulfur-containing methanol-rich liquid is subjected to flash distillation treatment II.
  • the conditions of the flash evaporation treatment I are: the control pressure is 0.32-0.34MPa;
  • the conditions of flashing treatment II are as follows: the control pressure is 0.32 ⁇ 0.34MPa.
  • sulfur-containing methanol-rich liquid passed into the desorption column segment CO 2 D-1 before, further comprising:
  • the temperature of the sulfur-containing methanol-rich liquid is raised to -35 to -45°C.
  • the remaining sulfur-containing methanol-rich liquid is heated to -25 to -35°C.
  • washing rich liquid refers to the solution obtained after low-temperature methanol washes the acid gases CO 2 , H 2 S, etc. in the feed gas, and is a methanol liquid rich in CO 2 and H 2 S.
  • the methanol-rich flash tank in the prior art is directly arranged at the bottom of the CO 2 stripping tower, that is, by adding a new D-1 section (the prior art) in the CO 2 stripping tower.
  • the methanol-rich flash tank has a role in prior art section only in the flash tank while the a-1, B-1, C-1 elevation upwards, reducing the CO 2 stripper column
  • the position difference between the discharge ports of A-1, B-1, and C-1 and the feed ports of A-1, B-1, and C-1 of the H 2 S concentration tower reduces the flow between the two towers. resistance.
  • FIG. 1 is a schematic diagram of a low-temperature methanol washing and washing rich liquid CO 2 desorption device and a process flow diagram in an embodiment of the present application.
  • T-101.CO 2 desorption tower T-102.H 2 S concentration tower, E-101. 1# heat exchanger, E-102. 2# heat exchanger, P101. 1# pump, P102. 2# pump ;
  • a low-temperature methanol washing and washing rich liquid CO 2 desorption device has a structure as shown in Figure 1:
  • CO 2 desorption tower T-101 includes A-1 section, B-1 section, C-1 section and D-1 sequentially arranged from top to bottom Section
  • H 2 S concentration tower T-102 includes A-2 section, B-2 section, C-2 section arranged in sequence from top to bottom.
  • the lower part of the A-1 section is connected with the upper part of the A-2 section through a pipeline;
  • the lower part of the B-1 section is connected with the middle part of the B-2 section through a pipeline; the lower part of the B-2 section is connected with the upper part of the C-1 section through a pipeline;
  • the lower part of the C-1 section is connected with the upper part of the C-2 section through a pipeline;
  • the top of the C-1 section and the top of the B-1 section are provided with a gas outlet II connected to the B-1 section and the A-1 section respectively;
  • the top of the C-1 section is provided with a gas outlet III that communicates with the B-2 section;
  • section A-1, the top of section A-2 and the upper part of section B-2 are all provided with air outlet IV;
  • the upper part of the A-1 section is provided with a liquid inlet I; the lower part of the A-2 section is provided with a liquid outlet I;
  • Liquid inlet II is set in the middle of section B-1;
  • the lower part of the C-2 section is provided with a stripping gas inlet, and the bottom of the C-2 section is provided with a liquid outlet II.
  • the lower part of the A-1 section is connected with the upper part of the B-1 section through a pipeline;
  • the bottom of the A-2 section is connected with the upper part of the B-2 section through a pipeline.
  • a 1# pump P-101 and a 1# heat exchanger E-101 are arranged on the pipeline connecting the H 2 S concentration tower T-102 with the D-1 section.
  • a 2# pump P-101 and a 2# heat exchanger E-102 are arranged on the pipeline connecting the D-1 section and the C-1 section.
  • the sulfur-rich methanol 2 after the medium pressure flash is decompressed and then enters the lower part of the T-101 B-1 section of the CO 2 desorption tower, where the dissolved CO 2 is flashed out, and the dissolved H 2 S is also partially flashed out.
  • the sulfur-free and rich methanol 1 after the medium pressure flash is decompressed and then enters the CO 2 desorption tower T-101 A-1 section, and the dissolved CO 2 is flashed out.
  • CO 2 desorption column T-101 overhead product obtained qualified CO 2 gas 3; CO 2 desorption column after methanol was flashed sulfur T-101 B-1 section 7 enters the H 2 S concentration column T-102 B-2 middle of the segment.
  • H 2 S concentration tower T-102 Sulfur-free rich methanol liquid after low-pressure flashing in section A-2, part of which is used as semi-lean liquid 11, and the other part is returned to H 2 S concentration tower T with sulfur-free rich methanol 9 as tail gas scrubbing -102
  • the upper part of the B-2 section wash the sulfur-containing gas flashed out of the sulfur-containing rich liquid.
  • the tail gas 12 with qualified hydrogen sulfide content is obtained from the upper part of the B-2 section of the H 2 S concentration tower T-102.
  • the low-temperature sulfur-containing methanol-rich liquid 13 obtained by stripping and flashing at the lower part of the B-2 section of the H 2 S concentration tower T-102 is heated through the 1# pump P-101 and the 1# heat exchanger E-101 (the temperature is raised to -35 ⁇ -45°C) into the CO 2 desorption tower T-101 D-1 section, the sulfur-rich methanol liquid after heating can be flashed (that is, flash treatment I, the flashing process is controlled at a pressure of 0.32 ⁇ 0.34MPa) to get out part of the CO 2 gas.
  • flash ie, flash treatment II, the control pressure of the flash process is 0.32-0.34MPa
  • the operating pressure of the T-101 tower is 0.1-0.12 MPa higher than the operating pressure of the T-102 tower, and the pressure difference serves as the driving force for the flow of methanol-rich liquids 6, 7, and 8 between the two towers.
  • the resistance that the flow needs to overcome is the pressure drop in the pipeline, the valve and the head position difference between the two towers.
  • the liquid outlets 1A, 1B, and 1C corresponding to the A-1, B-1, and C-1 sections of the T-101 tower are lower than those of the T-102 tower A-2, B-2, and C-2, respectively.
  • the liquid inlets 2A, 2B and 2C are about 10 to 15 meters away.
  • the low-temperature sulfur-rich methanol liquid 13 obtained in the C-2 section of the T-102 tower needs to be flashed in a separate flash tank.
  • the flash tank used in the prior art is basically a horizontal flash tank, which occupies a large area. ; and also need to connect a larger flash gas pipeline into the T-101 tower.
  • the D-1 section is added at the bottom of the T-101 tower, which plays the role of a flash tank; and after the D-1 section is added, the corresponding A-1, B-1, and C-1 sections are raised upward by 8 ⁇ 10 meters.
  • the improved low temperature methanol washing process has the following advantages:
  • T-101 and V-101 are a temperature and pressure system.
  • the flash tank is used as the D-1 section of the T-101 tower.
  • the equipment operating temperature, operating pressure and equipment material remain unchanged. Operation has no impact and does not increase system power consumption.

Abstract

一种低温甲醇洗洗涤富液CO2解吸装置和方法，装置包括CO2解吸塔和H2S浓缩塔；CO2解吸塔自上而下设置有C-1段和D-1段；D-1段分别与H2S浓缩塔和C-1段连通，用于对H2S浓缩塔中的经闪蒸处理后的含硫富甲醇液继续进行闪蒸处理。

Description

一种低温甲醇洗洗涤富液CO 2解吸装置及方法 技术领域
本申请涉及一种低温甲醇洗洗涤富液CO 2解吸装置及方法。
背景技术
低温甲醇洗工艺被广泛应用于以煤(石油焦)或渣油为原料生产合成氨、城市煤气、工业氢、合成甲醇或其他一些碳化学品的装置中。其过程为用甲醇吸收混合气中的酸性气，通常为CO 2或CO 2和H 2S，再经减压解吸、气提、加热使甲醇与酸性气分开，达到分离回收的目的。甲醇对酸性气的吸收能力随着温度的升高而降低。为提高甲醇对酸性气的吸收能力，减少溶剂循环量，必须维持甲醇洗装置在低温下操作。现有技术中，通过CO 2解吸塔和H 2S浓缩塔之间的压差推动富甲醇液的流动，但是通常两塔之间的压差很小，而两塔连接管口之间还存在一定的位差(CO 2解吸塔管口低而H 2S浓缩塔管口高)，如管道阻力过大会导致富甲醇液流动不畅，甲醇循环过程无法正常进行的问题。
发明内容
为了解决上述技术问题，本申请提供了一种低温甲醇洗洗涤富液CO 2解吸装置及方法，通过在CO 2解吸塔底部增加D-1段，利用D-1段对富甲醇进行闪蒸，同时提高了原CO 2解吸塔A-1、B-1、C-1段的高度，减少与H 2S浓缩塔对应管口的位差，保证了两塔富甲醇流动通畅。
为实现上述目的，本申请采用的技术方案如下：
本申请提出了一种低温甲醇洗洗涤富液CO 2解吸装置，包括CO 2解吸塔和H 2S浓缩塔；
CO 2解吸塔自上而下设置有C-1段和D-1段；
D-1段分别与H 2S浓缩塔和C-1段连通，用于对H 2S浓缩塔中的经闪蒸处理后的含硫富甲醇液继续进行闪蒸处理。
可选地，设置在H 2S浓缩塔中部的出液口与CO 2解吸塔D-1段的进液口连通，用于使H 2S浓缩塔中气提后的含硫富甲醇液进入D-1段中，进行闪蒸处理 Ⅰ；
D-1段的顶部设有与C-1段连通的气体出口Ⅰ，用于将经过闪蒸处理Ⅰ得到的CO 2闪蒸气通入C-1段；
D-1段的底部设有与C-1段连通的液体出口，用于将经过闪蒸处理Ⅰ得到的剩余含硫富甲醇液通入C-1段进行闪蒸处理Ⅱ。
可选地，CO 2解吸塔还包括A-1段和B-1段，A-1段位于B-1段的上方，B-1段位于C-1段的上方；
A-1段下部与A-2段上部通过管道连接；
B-1段下部与B-2段中部通过管道连接；B-2段下部与C-1段上部通过管道连接；
C-1段下部与C-2段上部通过管道连接；
具体地，A-1段上部设置有进液口Ⅰ；B-1段中部设置进液口Ⅱ；
C-1段的顶部、B-1段顶部设有分别与B-1段、A-1段连通的气体出口Ⅱ；
A-1段顶部、A-2段顶部、B-2段上部均设置有出气口Ⅲ；
A-2段下部设置有出液口Ⅰ；
C-2段下部设置有汽提气入口，C-2段底部设置有出液口Ⅱ；
优选地，A-1段下部与B-1段上部通过管道连接；
优选地，A-2段底部与B-2段上部通过管路连接。
可选地，D-1段的高度为8～10米。
可选地，H 2S浓缩塔与D-1段连通的管路上设置有输送泵和换热器。
可选地，D-1段与C-1段连通的管路上设置有输送泵和换热器。
本申请另一方面，提出了一种低温甲醇洗洗涤富液CO 2解吸方法，包括以下步骤：
将H 2S浓缩塔中气提后的含硫富甲醇液通入CO 2解吸塔D-1段进行闪蒸处理Ⅰ，得到CO 2闪蒸气和剩余含硫富甲醇液；
将CO 2闪蒸气通入CO 2解吸塔C-1段，回收CO 2闪蒸气；
将剩余含硫富甲醇液通入CO 2解吸塔C-1段，使得剩余含硫富甲醇液进行闪蒸处理Ⅱ。
可选地，闪蒸处理Ⅰ的条件为：控制压力在0.32～0.34MPa；
闪蒸处理Ⅱ的条件为：控制压力在0.32～0.34MPa。
可选地，将含硫富甲醇液通入CO 2解吸塔D-1段前，还包括：
对含硫富甲醇液进行换热升温；
优选地，将含硫富甲醇液升温至-35～-45℃。
可选地，将剩余含硫富甲醇液通入CO 2解吸塔C-1段前，还包括：
对剩余含硫富甲醇液进行换热升温；
优选地，将剩余含硫富甲醇液升温至-25～-35℃。
本申请中，“洗涤富液”是指低温甲醇洗涤原料气中酸性气体CO 2、H 2S等后的溶液，为富含CO 2、H 2S的甲醇液。
本申请能产生的有益效果包括：
1)本申请所提供的低温甲醇洗工艺，将现有技术中的富甲醇闪蒸罐直接设置在CO 2解吸塔的底部，即通过在CO 2解吸塔新增D-1段(现有技术中的富甲醇闪蒸罐)，D-1段不仅具有现有工艺中闪蒸罐的作用，同时使A-1、B-1、C-1段向上抬高，减小了CO 2解吸塔A-1、B-1、C-1段出料口与H 2S浓缩塔A-1、B-1、C-1段进料口之间的位差，降低了两塔之间的流动阻力。同时本申请中，对现有技术中闪蒸罐的直接利用，无需设置额外的增高装置，节约了设备成本。
2)本申请所提供的低温甲醇洗工艺，通过在CO 2解吸塔新增D-1段，将闪蒸罐所需的外部工艺管线，改成了塔内升气帽，降低了低温管线成本。
3)本申请所提供的低温甲醇洗工艺，通过在CO 2解吸塔新增D-1段，与原富甲醇闪蒸罐相比，设备操作温度、操作压力及设备材质不变，对全流程操作无影响，不增加系统消耗。
附图说明
图1为本申请一种实施方式中低温甲醇洗洗涤富液CO 2解吸装置和工艺流程示意图。
部件和附图标记列表：
T-101.CO 2解吸塔，T-102.H 2S浓缩塔，E-101. 1#换热器，E-102. 2#换热器， P101. 1#泵，P102. 2#泵；
1.无硫富甲醇，2.含硫富甲醇，3.CO 2产品气，4.A-1段闪蒸后的无硫富甲醇，5.CO 2气洗涤用无硫富甲醇，6.去H 2S浓缩塔无硫富甲醇液，7.B-1段闪蒸后的含硫甲醇，8.C-1段闪蒸后的含硫富甲醇，9.尾气洗涤用无硫富甲醇，10.低压CO 2气，11.半贫液，12.尾气，13.低温含硫富甲醇，14.低压氮气，15.气提后的含硫甲醇，16.CO 2闪蒸气，17.D-1段闪蒸后的含硫甲醇。
具体实施方式
下面结合实施例详述本申请，但本申请并不局限于这些实施例。
本申请一种实施方式中一种低温甲醇洗洗涤富液CO 2解吸装置，其结构如图1所示：
包括CO 2解吸塔T-101和H 2S浓缩塔T-102，CO 2解吸塔T-101包括自上而下依次设置A-1段、B-1段、C-1段和D-1段，H 2S浓缩塔T-102包括自上而下依次设置A-2段、B-2段、C-2段。
A-1段下部与A-2段上部通过管道连接；
B-1段下部与B-2段中部通过管道连接；B-2段下部与C-1段上部通过管道连接；
C-1段下部与C-2段上部通过管道连接；
C-1段的顶部、B-1段顶部设有分别与B-1段、A-1段连通的气体出口Ⅱ；
C-1段的顶部设有与B-2段连通的气体出口Ⅲ；
A-1段顶部、A-2段顶部、B-2段上部均设置有出气口Ⅳ；
A-1段上部设置有进液口Ⅰ；A-2段下部设置有出液口Ⅰ；
B-1段中部设置进液口Ⅱ；
C-2段下部设置有汽提气入口，C-2段底部设置有出液口Ⅱ。
A-1段下部与B-1段上部通过管道连接；
A-2段底部与B-2段上部通过管路连接。
H 2S浓缩塔T-102与D-1段连通的管路上设置有1#泵P-101和1#换热器E-101。
D-1段与C-1段连通的管路上设置有2#泵P-101和2#换热器E-102。
本申请低温甲醇洗洗涤富液CO 2解吸方法，其工艺流程如图1所示：
中压闪蒸后的含硫富甲醇2经减压后进入CO 2解吸塔T-101 B-1段下部，闪蒸出溶解的CO 2，同时溶解的H 2S也部分闪蒸出来。中压闪蒸后的无硫富甲醇1经减压后进入CO 2解吸塔T-101 A-1段，闪蒸出溶解的CO 2。CO 2解吸塔T-101 A-1段闪蒸后的无硫富甲醇液4中，其中一部分作为CO 2气洗涤用无硫富甲醇5返回CO 2解吸塔T-101 B-1段，洗涤塔内含硫富液闪蒸出的含硫气体；另一部分作为去H 2S浓缩塔无硫富甲醇液6进入H 2S浓缩塔T-102 A-2段。CO 2解吸塔T-101塔顶得到合格的CO 2产品气3；CO 2解吸塔T-101 B-1段闪蒸后的含硫甲醇液7进入H 2S浓缩塔T-102 B-2段中部。H 2S浓缩塔T-102 A-2段低压闪蒸后的无硫富甲醇液，其中一部分用作为半贫液11，另一部分作为尾气洗涤用无硫富甲醇9返回H 2S浓缩塔T-102 B-2段上部，洗涤含硫富液闪蒸出的含硫气体。H 2S浓缩塔T-102 B-2段上部得到硫化氢含量合格的尾气12。H 2S浓缩塔T-102 B-2段下部气提闪蒸得到的低温含硫富甲醇液13通过1#泵P-101、经1#换热器E-101升温后(升温至-35～-45℃)进入CO 2解吸塔T-101 D-1段，升温后的含硫富甲醇液可以闪蒸(即闪蒸处理Ⅰ，闪蒸过程控制压力在0.32～0.34MPa)出部分CO 2气体。CO 2解吸塔T-101 D-1段的CO 2闪蒸气16进入CO 2解吸塔T-101 C-1段；CO 2解吸塔T-101 D-1段闪蒸后的含硫富甲醇17(即剩余含硫富甲醇)通过2#泵P-102、经2#换热器E-102升温后(升温至-25～-35℃)进入CO 2解吸塔T-101 C-1段，继续闪蒸(即闪蒸处理Ⅱ，闪蒸过程控制压力在0.32～0.34MPa)CO 2气体，闪蒸气经CO 2解吸塔T-101 B-1段洗涤后进CO 2产品气。CO 2解吸塔T-101 C-1段闪蒸后的含硫富甲醇液8进入H 2S浓缩塔T-102 C-2段，H 2S浓缩塔T-102 C-2段通入低压氮气14气提，H 2S浓缩塔T-102塔底得到的气提后含硫富甲醇15去热再生系统。H 2S浓缩塔T-102闪蒸得到的低压CO 2气10从塔顶排出。
现有工艺中T-101塔操作压力比T-102塔操作压力高0.1～0.12MPa，压差作为两个塔之间富甲醇液6、7、8流动的推动力。流动需要克服的阻力是管道、阀门压降和两塔管口的位差。而T-101塔A-1段、B-1段、C-1段对应的出液口1A、1B、1C分别低于T-102塔A-2段、B-2段、C-2段的进液口2A、2B、2C约10～15米，当管道、阀门压降偏大时，常发生T-101塔富甲醇到T-102塔流动不畅的情况，造成装置无法正常操作；
同时T-102塔C-2段得到低温含硫富甲醇液13需要单独进入的闪蒸罐中进 行闪蒸，现有技术中采用的闪蒸罐基本为卧式闪蒸罐，占地较大；且另需要接一条较大的闪蒸气管线进入T-101塔。
本申请通过在T-101塔底部新增D-1段，起到了闪蒸罐的作用；并且增加D-1段后，相应的A-1、B-1、C-1段向上抬高8～10米。改进后的低温甲醇洗工艺具有以下优点：
1)减小了T-101塔管口1A、1B、1C与T-102塔管口2A、2B、2C的位差，降低的流动阻力；
2)将卧式闪蒸罐采用T-101塔D-1段代替，节省占地，同时将闪蒸罐所需的外部CO 2闪蒸气管线，改为塔内升气，节省管线费用，降低了管线成本；
3)从流程看T-101与V-101本身就是一个温度、压力体系，将闪蒸罐作为T-101塔D-1段，设备操作温度、操作压力及设备材质不变，同时对全流程操作无影响，不增加系统能耗。
以上所述，仅是本申请的几个实施例，并非对本申请做任何形式的限制，虽然本申请以较佳实施例揭示如上，然而并非用以限制本申请，任何熟悉本专业的技术人员，在不脱离本申请技术方案的范围内，利用上述揭示的技术内容做出些许的变动或修饰均等同于等效实施案例，均属于技术方案范围内。

Claims (12)

  1. 一种低温甲醇洗洗涤富液CO 2解吸装置，其特征在于，所述装置包括CO 2解吸塔和H 2S浓缩塔；
    所述CO 2解吸塔自上而下设置有C-1段和D-1段；
    所述D-1段分别与所述H 2S浓缩塔和所述C-1段连通，用于对所述H 2S浓缩塔中的经闪蒸处理后的含硫富甲醇液继续进行闪蒸处理。
  2. 根据权利要求1所述的低温甲醇洗洗涤富液CO 2解吸装置，其特征在于，设置在所述H 2S浓缩塔中部的出液口与所述CO 2解吸塔D-1段的进液口连通，用于使所述H 2S浓缩塔中气提后的含硫富甲醇液进入所述D-1段中，进行闪蒸处理Ⅰ；
    所述D-1段的顶部设有与所述C-1段连通的气体出口Ⅰ，用于将经过闪蒸处理Ⅰ得到的CO 2闪蒸气通入所述C-1段；
    所述D-1段的底部设有与所述C-1段连通的液体出口，用于将经过闪蒸处理Ⅰ得到的剩余含硫富甲醇液通入所述C-1段进行闪蒸处理Ⅱ。
  3. 根据权利要求1所述的低温甲醇洗洗涤富液CO 2解吸装置，其特征在于，所述CO 2解吸塔还包括A-1段和B-1段，所述A-1段位于所述B-1段的上方，所述B-1段位于所述C-1段的上方；
    所述H 2S浓缩塔自上而下依次设置A-2段、B-2段和C-2段；
    所述A-1段下部与所述A-2段上部通过管道连接；
    所述B-1段下部与所述B-2段中部通过管道连接；所述B-2段下部与所述C-1段上部通过管道连接；
    所述C-1段下部与所述C-2段上部通过管道连接。
  4. 根据权利要求1所述的低温甲醇洗洗涤富液CO 2解吸装置，其特征在于，所述D-1段的高度为8～10米。
  5. 根据权利要求1所述的低温甲醇洗洗涤富液CO 2解吸装置，其特征在于，所述H 2S浓缩塔与所述D-1段连通的管路上设置有输送泵和换热器。
  6. 根据权利要求1所述的低温甲醇洗洗涤富液CO 2解吸装置，其特征在于，所述D-1段与所述C-1段连通的管路上设置有输送泵和换热器。
  7. 一种低温甲醇洗洗涤富液CO 2解吸方法，其特征在于，包括以下步骤：
    将H 2S浓缩塔中气提后的含硫富甲醇液通入CO 2解吸塔D-1段进行闪蒸处理Ⅰ，得到CO 2闪蒸气和剩余含硫富甲醇液；
    将所述CO 2闪蒸气通入所述CO 2解吸塔C-1段，回收所述CO 2闪蒸气；
    将所述剩余含硫富甲醇液通入所述CO 2解吸塔C-1段，使得所述剩余含硫富甲醇液进行闪蒸处理Ⅱ。
  8. 根据权利要求7所述的低温甲醇洗洗涤富液CO 2解吸方法，其特征在于，所述闪蒸处理Ⅰ的条件为：控制压力在0.32～0.34MPa；
    所述闪蒸处理Ⅱ的条件为：控制压力在0.32～0.34MPa。
  9. 根据权利要求7所述的低温甲醇洗洗涤富液CO 2解吸方法，其特征在于，将所述含硫富甲醇液通入CO 2解吸塔D-1段前，还包括：
    对所述含硫富甲醇液进行换热升温。
  10. 根据权利要求9所述的低温甲醇洗洗涤富液CO 2解吸方法，其特征在于，将所述含硫富甲醇液升温至-35～-45℃。
  11. 根据权利要求7所述的低温甲醇洗洗涤富液CO 2解吸方法，其特征在于，将所述剩余含硫富甲醇液通入所述CO 2解吸塔C-1段前，还包括：
    对所述剩余含硫富甲醇液进行换热升温。
  12. 根据权利要求11所述的低温甲醇洗洗涤富液CO 2解吸方法，其特征在于，将所述剩余含硫富甲醇液升温至-25～-35℃。
PCT/CN2020/110344 2020-06-30 2020-08-20 一种低温甲醇洗洗涤富液co 2解吸装置及方法 WO2022000735A1 (zh)

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Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1377825A (zh) * 2001-12-10 2002-11-06 大连理工大学 一种节能型原料气净化甲醇洗方法
US20090101007A1 (en) * 2004-10-08 2009-04-23 Rasmus Find Method for recovery of carbon dioxide from a gas
US7744751B2 (en) * 2005-05-12 2010-06-29 Battelle Memorial Institute Method of generating hydrocarbon reagents from diesel, natural gas and other logistical fuels
CN203639434U (zh) * 2013-12-06 2014-06-11 华南理工大学 一种低温甲醇洗工艺和co2压缩工艺的耦合系统
CN204211704U (zh) * 2014-10-27 2015-03-18 上海国际化建工程咨询公司 一种低温甲醇洗节能增产的装置
EP2939722A1 (en) * 2014-05-01 2015-11-04 Nederlandse Organisatie voor toegepast- natuurwetenschappelijk onderzoek TNO Gas desorption
CN105523524A (zh) * 2015-12-29 2016-04-27 大连百傲化学股份有限公司 一种生产高纯硫化氢的装置及工艺方法
CN108977236A (zh) * 2018-08-29 2018-12-11 国家能源投资集团有限责任公司 一种低温甲醇洗系统以及合成气的提供方法
CN208911769U (zh) * 2018-09-26 2019-05-31 内蒙古大唐国际克什克腾煤制天然气有限责任公司 降低甲醇洗co2闪蒸塔i段和h2s浓缩塔i段压力装置
CN210584343U (zh) * 2019-06-13 2020-05-22 辽宁大唐国际阜新煤制天然气有限责任公司 排放气净化装置

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1377825A (zh) * 2001-12-10 2002-11-06 大连理工大学 一种节能型原料气净化甲醇洗方法
US20090101007A1 (en) * 2004-10-08 2009-04-23 Rasmus Find Method for recovery of carbon dioxide from a gas
US7744751B2 (en) * 2005-05-12 2010-06-29 Battelle Memorial Institute Method of generating hydrocarbon reagents from diesel, natural gas and other logistical fuels
CN203639434U (zh) * 2013-12-06 2014-06-11 华南理工大学 一种低温甲醇洗工艺和co2压缩工艺的耦合系统
EP2939722A1 (en) * 2014-05-01 2015-11-04 Nederlandse Organisatie voor toegepast- natuurwetenschappelijk onderzoek TNO Gas desorption
CN204211704U (zh) * 2014-10-27 2015-03-18 上海国际化建工程咨询公司 一种低温甲醇洗节能增产的装置
CN105523524A (zh) * 2015-12-29 2016-04-27 大连百傲化学股份有限公司 一种生产高纯硫化氢的装置及工艺方法
CN108977236A (zh) * 2018-08-29 2018-12-11 国家能源投资集团有限责任公司 一种低温甲醇洗系统以及合成气的提供方法
CN208911769U (zh) * 2018-09-26 2019-05-31 内蒙古大唐国际克什克腾煤制天然气有限责任公司 降低甲醇洗co2闪蒸塔i段和h2s浓缩塔i段压力装置
CN210584343U (zh) * 2019-06-13 2020-05-22 辽宁大唐国际阜新煤制天然气有限责任公司 排放气净化装置

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