CN109999618B - System and method for separating carbon dioxide from medium-high pressure gas source - Google Patents
System and method for separating carbon dioxide from medium-high pressure gas source Download PDFInfo
- Publication number
- CN109999618B CN109999618B CN201910340516.3A CN201910340516A CN109999618B CN 109999618 B CN109999618 B CN 109999618B CN 201910340516 A CN201910340516 A CN 201910340516A CN 109999618 B CN109999618 B CN 109999618B
- Authority
- CN
- China
- Prior art keywords
- pressure
- gas
- lean liquid
- tower
- low
- Prior art date
- Legal status (The legal status 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 status listed.)
- Active
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
本发明提供的一种中高压气源中二氧化碳的分离系统及方法，来自吸收塔的CO2富液通过闪蒸、高压解吸、低压解吸等方式逐级减压再生，充分利用了CO2气源的压力较高的特点，减少了外来热耗的输入；满足了低能耗和低成本要求；高压解吸塔塔顶的高温解吸气通入低压解吸塔的再沸器，用作加热解吸的热源，减少了低压解吸塔所需的外来热耗，同时降低了解吸气冷却器的冷却水消耗量；来自高压解吸塔和低压解吸塔的贫液和半贫液分别从吸收塔上段填料和中段填料进入，有助于保持塔身各处反应温度较为均匀，避免局部温度过高，减少吸收剂降解和损耗；本发明充分利用了CO2气源的压力较高的特点，减少了外来热耗的输入；满足了低能耗和低成本要求。
The present invention provides a system and method for separating carbon dioxide from a medium- and high-pressure gas source. The CO2- rich liquid from an absorption tower is regenerated by stepwise decompression through flash evaporation, high-pressure desorption, low-pressure desorption and the like, which fully utilizes the high-pressure characteristic of the CO2 gas source and reduces the input of external heat consumption; the requirements of low energy consumption and low cost are met; the high-temperature desorbed gas at the top of the high-pressure desorption tower is introduced into the reboiler of the low-pressure desorption tower and used as a heat source for heating and desorption, which reduces the external heat consumption required for the low-pressure desorption tower and reduces the cooling water consumption of the desorbed gas cooler; the lean liquid and semi-lean liquid from the high-pressure desorption tower and the low-pressure desorption tower enter from the upper and middle fillers of the absorption tower respectively, which helps to keep the reaction temperature of various parts of the tower body relatively uniform, avoid excessive local temperature, and reduce the degradation and loss of the absorbent; the present invention fully utilizes the high-pressure characteristic of the CO2 gas source and reduces the input of external heat consumption; the requirements of low energy consumption and low cost are met.
Description
技术领域Technical Field
本发明属于气体分离技术、二氧化碳减排技术领域，具体涉及一种中高压气源中二氧化碳的分离系统及方法。The present invention belongs to the field of gas separation technology and carbon dioxide emission reduction technology, and in particular relates to a system and method for separating carbon dioxide from a medium- and high-pressure gas source.
背景技术Background technique
燃煤电厂是我国CO2集中稳定的排放源，约占全国CO2总排放量的35%。此外，合成氨、制氢、煤气化、煤化工等工业领域也存在大量CO2捕集或分离过程。相比燃煤电厂烟道气，这些领域的脱碳工序所需处理的气体压力高（2MPa～5MPa），CO2浓度高（25～60%）。传统常压CO2分离工艺一般通过低温吸收、高温解吸的方法实现CO2脱除，或者通过热泵、机械蒸汽再压缩等手段回收部分热量，达到节能降耗的目的。但对于中高压CO2气源来说，常压CO2分离工艺无法充分利用中高压气源特点，很难充分满足其低能耗和低成本要求。Coal-fired power plants are a concentrated and stable source of CO2 emissions in China, accounting for about 35% of the country's total CO2 emissions. In addition, there are also a large number of CO2 capture or separation processes in industrial fields such as synthetic ammonia, hydrogen production, coal gasification, and coal chemical industry. Compared with the flue gas of coal-fired power plants, the gas pressure required for the decarbonization process in these fields is high (2MPa~5MPa) and the CO2 concentration is high (25~60%). The traditional atmospheric pressure CO2 separation process generally achieves CO2 removal through low-temperature absorption and high-temperature desorption, or recovers part of the heat through heat pumps, mechanical steam recompression and other means to achieve energy saving and consumption reduction. However, for medium and high pressure CO2 gas sources, the atmospheric pressure CO2 separation process cannot fully utilize the characteristics of medium and high pressure gas sources, and it is difficult to fully meet its low energy consumption and low cost requirements.
发明内容Summary of the invention
本发明的目的在于提供一种中高压气源中二氧化碳的分离系统及方法，解决了现有的常压CO2分离工艺无法实现中高压CO2的脱除。The purpose of the present invention is to provide a system and method for separating carbon dioxide from medium- and high-pressure gas sources, which solves the problem that the existing atmospheric pressure CO2 separation process cannot achieve the removal of medium- and high-pressure CO2 .
为了达到上述目的，本发明采用的技术方案是：In order to achieve the above object, the technical solution adopted by the present invention is:
本发明提供的一种中高压气源中二氧化碳的分离系统，包括吸收塔、闪蒸罐、高压解吸塔、高压解吸再沸器、低压解吸塔、贫液换热设备、半贫液换热设备、第二低压解吸再沸器、解吸气冷却器和气液分离器，其中，吸收塔的底部CO2富液出口连接闪蒸罐的入口，闪蒸罐的顶部解吸气体出口通过解吸气冷却器连接气液分离器的入口；The present invention provides a system for separating carbon dioxide from a medium- and high-pressure gas source, comprising an absorption tower, a flash tank, a high-pressure desorption tower, a high-pressure desorption reboiler, a low-pressure desorption tower, a lean liquid heat exchange device, a semi-lean liquid heat exchange device, a second low-pressure desorption reboiler, a desorption gas cooler and a gas-liquid separator, wherein the CO2- rich liquid outlet at the bottom of the absorption tower is connected to the inlet of the flash tank, and the desorption gas outlet at the top of the flash tank is connected to the inlet of the gas-liquid separator through the desorption gas cooler;
闪蒸罐的底部液相出口分为两路，一路连接高压解吸塔的入口；另一路连接低压解吸塔的入口；The bottom liquid phase outlet of the flash tank is divided into two paths, one path is connected to the inlet of the high-pressure desorption tower; the other path is connected to the inlet of the low-pressure desorption tower;
高压解吸塔的底部热贫液出口依次通过第二低压解吸再沸器和贫液换热设备连接吸收塔的顶部入口；高压解吸塔的顶部解吸气体出口通过解吸气冷却器连接气液分离器的入口；The hot lean liquid outlet at the bottom of the high-pressure desorption tower is connected to the top inlet of the absorption tower through the second low-pressure desorption reboiler and the lean liquid heat exchange equipment in sequence; the desorption gas outlet at the top of the high-pressure desorption tower is connected to the inlet of the gas-liquid separator through the desorption gas cooler;
高压解吸塔连接高压解吸再沸器；The high-pressure desorption tower is connected to the high-pressure desorption reboiler;
低压解吸塔的底部半贫液出口通过半贫液换热设备连接吸收塔的中部入口；低压解吸塔的顶部解吸气体出口通过解吸气冷却器连接气液分离器的入口；The semi-lean liquid outlet at the bottom of the low-pressure desorption tower is connected to the middle inlet of the absorption tower through the semi-lean liquid heat exchange equipment; the desorption gas outlet at the top of the low-pressure desorption tower is connected to the inlet of the gas-liquid separator through the desorption gas cooler;
低压解吸塔连接第二低压解吸再沸器；The low-pressure desorption tower is connected to a second low-pressure desorption reboiler;
气液分离器的底部冷凝液出口分别连接高压解吸塔和低压解吸塔的入口，气液分离器的顶部设置有CO2产品气出口；The condensate outlet at the bottom of the gas-liquid separator is connected to the inlet of the high-pressure desorption tower and the low-pressure desorption tower respectively, and the top of the gas-liquid separator is provided with a CO2 product gas outlet;
吸收塔的顶部设置有净化气出口。A purified gas outlet is provided at the top of the absorption tower.
优选地，贫液换热设备包括贫液换热器和贫液冷却器，其中，闪蒸罐底部液相出口的一路连接贫液换热器的冷端入口，贫液换热器的冷端出口连接高压解吸塔的入口；高压解吸塔的底部热贫液出口连接贫液换热器的热端入口，贫液换热器的热端出口通过贫液冷却器连接吸收塔的顶部入口。Preferably, the lean liquid heat exchange equipment includes a lean liquid heat exchanger and a lean liquid cooler, wherein one of the liquid phase outlets at the bottom of the flash tank is connected to the cold end inlet of the lean liquid heat exchanger, and the cold end outlet of the lean liquid heat exchanger is connected to the inlet of the high-pressure desorption tower; the hot lean liquid outlet at the bottom of the high-pressure desorption tower is connected to the hot end inlet of the lean liquid heat exchanger, and the hot end outlet of the lean liquid heat exchanger is connected to the top inlet of the absorption tower through the lean liquid cooler.
优选地，贫液换热器的热端出口与贫液冷却器之间设置有贫液泵。Preferably, a lean liquid pump is provided between the hot end outlet of the lean liquid heat exchanger and the lean liquid cooler.
优选地，半贫液换热设备包括半贫液换热器和半贫液冷却器，其中，闪蒸罐底部液相出口的另一路连接半贫液换热器的冷端入口，半贫液换热器的冷端出口连接低压解吸塔的入口；低压解吸塔的底部热贫液出口连接半贫液换热器的热端入口，半贫液换热器的热端出口通过半贫液换热器连接吸收塔的中部入口。Preferably, the semi-lean liquid heat exchange equipment includes a semi-lean liquid heat exchanger and a semi-lean liquid cooler, wherein another liquid phase outlet at the bottom of the flash tank is connected to the cold end inlet of the semi-lean liquid heat exchanger, and the cold end outlet of the semi-lean liquid heat exchanger is connected to the inlet of the low-pressure desorption tower; the hot lean liquid outlet at the bottom of the low-pressure desorption tower is connected to the hot end inlet of the semi-lean liquid heat exchanger, and the hot end outlet of the semi-lean liquid heat exchanger is connected to the middle inlet of the absorption tower through the semi-lean liquid heat exchanger.
优选地，半贫液换热器的热端出口和半贫液冷却器之间设置有半贫液泵。Preferably, a semi-lean liquid pump is provided between the hot end outlet of the semi-lean liquid heat exchanger and the semi-lean liquid cooler.
优选地，高压解吸再沸器连接外接热源设备。Preferably, the high-pressure desorption reboiler is connected to an external heat source device.
优选地，低压解吸塔还分别连接有第一低压解吸再沸器，第一低压解吸再沸器连接外接热源设备。Preferably, the low-pressure desorption tower is also connected to a first low-pressure desorption reboiler, and the first low-pressure desorption reboiler is connected to an external heat source device.
一种中高压气源中二氧化碳的分离方法，基于一种中高压气源中二氧化碳的分离系统，包括以下步骤：A method for separating carbon dioxide from a medium- and high-pressure gas source, based on a system for separating carbon dioxide from a medium- and high-pressure gas source, comprises the following steps:
含有CO2的工业气从吸收塔的下部进入吸收塔与从不同位置加入的贫液、半贫液逆流接触，完成吸收脱除CO2过程，脱除CO2后的净化气从吸收塔顶部排出；Industrial gas containing CO2 enters the absorption tower from the bottom of the absorption tower and contacts with lean liquid and semi-lean liquid added from different positions in countercurrent to complete the absorption and removal of CO2 . The purified gas after CO2 removal is discharged from the top of the absorption tower.
吸收塔的底部排出的CO2富液进入闪蒸罐进行初步减压解吸，闪蒸罐顶部排出的解吸气体经过解吸气冷却器进入气液分离器；The CO2- rich liquid discharged from the bottom of the absorption tower enters the flash tank for initial decompression and desorption, and the desorbed gas discharged from the top of the flash tank passes through the desorbed gas cooler and enters the gas-liquid separator;
闪蒸罐底部的排出液相分两路，一路进入高压解吸塔进行解吸，另一部进入低压解吸塔进行解吸；The discharged liquid phase at the bottom of the flash tank is divided into two paths, one enters the high-pressure desorption tower for desorption, and the other enters the low-pressure desorption tower for desorption;
高压解吸塔底部的热贫液通过贫液换热设备进行降温，之后送往吸收塔的顶部循环使用；The hot lean liquid at the bottom of the high-pressure desorption tower is cooled by the lean liquid heat exchange equipment and then sent to the top of the absorption tower for recycling;
高压解吸塔通过高压解吸再沸器加热，其塔顶的解吸气体进入解吸气冷却器进一步冷凝后进入气液分离器；The high-pressure desorption tower is heated by a high-pressure desorption reboiler, and the desorption gas at the top of the tower enters the desorption gas cooler for further condensation and then enters the gas-liquid separator;
低压解吸塔通过第二低压解吸再沸器加热，其底部的半贫液经半贫液换热设备进行降温，之后返回吸收塔的中部循环使用；The low-pressure desorption tower is heated by the second low-pressure desorption reboiler, and the semi-lean liquid at the bottom is cooled by the semi-lean liquid heat exchange equipment, and then returned to the middle of the absorption tower for recycling;
低压解吸塔塔顶的解吸气体经解吸气冷却器进一步冷凝后进入气液分离器；The desorbed gas at the top of the low-pressure desorber is further condensed by the desorbed gas cooler and then enters the gas-liquid separator;
气液分离器底部的冷凝液分别返回高压解吸塔和低压解吸塔；气液分离器上部的气体出口为CO2产品气。The condensate at the bottom of the gas-liquid separator is returned to the high-pressure desorption tower and the low-pressure desorption tower respectively; the gas outlet at the top of the gas-liquid separator is the CO2 product gas.
与现有技术相比，本发明的有益效果是：Compared with the prior art, the present invention has the following beneficial effects:
本发明提供的一种中高压气源中二氧化碳的分离系统，来自吸收塔的CO2富液通过闪蒸、高压解吸、低压解吸等方式逐级减压再生，充分利用了CO2气源的压力较高的特点，减少了外来热耗的输入；满足了低能耗和低成本要求。The present invention provides a system for separating carbon dioxide from medium- and high-pressure gas sources. The CO2- rich liquid from the absorption tower is regenerated by stepwise pressure reduction through flash evaporation, high-pressure desorption, low-pressure desorption, etc., which fully utilizes the high pressure characteristic of the CO2 gas source and reduces the input of external heat consumption, thereby meeting the requirements of low energy consumption and low cost.
进一步的，高压解吸塔塔顶的高温解吸气通入低压解吸塔的再沸器，用作加热解吸的热源，减少了低压解吸塔所需的外来热耗，同时降低了解吸气冷却器的冷却水消耗量。Furthermore, the high-temperature desorbed gas at the top of the high-pressure desorber is introduced into the reboiler of the low-pressure desorber and used as a heat source for heating desorption, thereby reducing the external heat consumption required by the low-pressure desorber and reducing the cooling water consumption of the desorbed gas cooler.
进一步的，来自高压解吸塔和低压解吸塔的贫液和半贫液分别从吸收塔上段填料和中段填料进入，有助于保持塔身各处反应温度较为均匀，避免局部温度过高，减少吸收剂降解和损耗。Furthermore, the lean liquid and semi-lean liquid from the high-pressure desorption tower and the low-pressure desorption tower enter from the upper and middle fillers of the absorption tower respectively, which helps to maintain a relatively uniform reaction temperature throughout the tower body, avoid excessive local temperature, and reduce absorbent degradation and loss.
进一步的，根据分离工艺的中高压特点和系统内的热能品位特性进行能量的优化利用，没有引入热泵、机械蒸汽再压缩等热回收设备，有效降低投资成本和操作成本。Furthermore, energy is optimized based on the medium and high pressure characteristics of the separation process and the thermal energy grade characteristics within the system, without introducing heat recovery equipment such as heat pumps and mechanical vapor recompression, effectively reducing investment and operating costs.
附图说明BRIEF DESCRIPTION OF THE DRAWINGS
图1是本发明涉及的分离系统的结构示意图。FIG. 1 is a schematic structural diagram of a separation system according to the present invention.
具体实施方式Detailed ways
下面结合附图，对本发明进一步详细说明。The present invention will be further described in detail below in conjunction with the accompanying drawings.
如图1所示，本发明提供的一种中高压气源中二氧化碳的分离系统，包括吸收塔1、闪蒸罐2、贫液换热器3、高压解吸塔4、高压解吸再沸器5、贫液泵6、贫液冷却器7、半贫液换热器8、低压解吸塔9、半贫液泵10、半贫液冷却器11、第一低压解吸再沸器12、第二低压解吸再沸器13、解吸气冷却器14、气液分离器15和冷凝液泵16，其中，吸收塔1的气体进口与含CO2的工业气气源相连，吸收塔1的富液出口与闪蒸罐2的溶液进口相连；闪蒸罐2底部的溶液出口分两路，一路通过贫液换热器3与高压解吸塔4上部的溶液进口相连；高压解吸塔4设置高压解吸再沸器5，由外来蒸汽提供热源；高压解吸塔4底部贫液出口依次通过贫液换热器3、贫液泵6、贫液冷却器7与吸收塔1上部的贫液进口相连；As shown in FIG1 , a system for separating carbon dioxide from a medium- and high-pressure gas source provided by the present invention comprises an absorption tower 1, a flash tank 2, a lean liquid heat exchanger 3, a high-pressure desorption tower 4, a high-pressure desorption reboiler 5, a lean liquid pump 6, a lean liquid cooler 7, a semi-lean liquid heat exchanger 8, a low-pressure desorption tower 9, a semi-lean liquid pump 10, a semi-lean liquid cooler 11, a first low-pressure desorption reboiler 12, a second low-pressure desorption reboiler 13, a desorption gas cooler 14, a gas-liquid separator 15 and a condensate pump 16, wherein the gas inlet of the absorption tower 1 is connected to the gas containing CO 2 is connected to the industrial gas source, the rich liquid outlet of the absorption tower 1 is connected to the solution inlet of the flash tank 2; the solution outlet at the bottom of the flash tank 2 is divided into two paths, one of which is connected to the solution inlet at the top of the high-pressure desorption tower 4 through the lean liquid heat exchanger 3; the high-pressure desorption tower 4 is provided with a high-pressure desorption reboiler 5, and the heat source is provided by external steam; the lean liquid outlet at the bottom of the high-pressure desorption tower 4 is connected to the lean liquid inlet at the top of the absorption tower 1 through the lean liquid heat exchanger 3, the lean liquid pump 6, and the lean liquid cooler 7 in sequence;
闪蒸罐2底部的溶液出口另一路通过半贫液换热器8与低压解吸塔9的上部和中部溶液进口相连；低压解吸塔9底部的半品液出口依次通过半贫液换热器8、半贫液泵10、半贫液冷却器11与吸收塔1中部的半贫液进口相连；Another solution outlet at the bottom of the flash tank 2 is connected to the upper and middle solution inlets of the low-pressure desorption tower 9 through the semi-lean liquid heat exchanger 8; the semi-product liquid outlet at the bottom of the low-pressure desorption tower 9 is connected to the semi-lean liquid inlet in the middle of the absorption tower 1 through the semi-lean liquid heat exchanger 8, the semi-lean liquid pump 10, and the semi-lean liquid cooler 11 in sequence;
低压解吸塔9设置第一低压解吸再沸器12和第二低压解吸再沸器13；第一低压解吸再沸器12由外来蒸汽提供热源，第二低压解吸再沸器13由来自高压解吸塔4顶部的解吸气提供热源；The low-pressure desorption tower 9 is provided with a first low-pressure desorption reboiler 12 and a second low-pressure desorption reboiler 13; the first low-pressure desorption reboiler 12 is provided with a heat source by external steam, and the second low-pressure desorption reboiler 13 is provided with a heat source by the desorption gas from the top of the high-pressure desorption tower 4;
来自闪蒸罐2顶部、高压解吸塔4顶部和低压解吸塔9顶部的解吸气体经过解吸气冷却器14与气液分离器15的进口相连；气液分离器15底部的冷凝液出口通过冷凝液泵16分别与高压解吸塔4上部和低压解吸塔9上部的冷凝液进口相连，气液分离器15上部的气体出口为二氧化碳产品气出口。The desorbed gas from the top of the flash tank 2, the top of the high-pressure desorption tower 4 and the top of the low-pressure desorption tower 9 is connected to the inlet of the gas-liquid separator 15 through the desorption gas cooler 14; the condensate outlet at the bottom of the gas-liquid separator 15 is connected to the condensate inlets of the upper part of the high-pressure desorption tower 4 and the upper part of the low-pressure desorption tower 9 through the condensate pump 16, and the gas outlet at the upper part of the gas-liquid separator 15 is the carbon dioxide product gas outlet.
本发明的工作原理如下：The working principle of the present invention is as follows:
含有CO2的工业气从吸收塔1的下部进入吸收塔与从不同位置加入的吸收剂贫液、半贫液逆流接触，完成吸收脱除CO2过程，脱除CO2后的净化气从吸收塔1顶部排出。The industrial gas containing CO2 enters the absorption tower from the lower part of the absorption tower 1 and countercurrently contacts with the absorbent lean liquid and semi-lean liquid added from different positions to complete the absorption and CO2 removal process. The purified gas after CO2 removal is discharged from the top of the absorption tower 1.
来自贫液冷却器7的贫液从最上一段填料的上部加入，来自半贫液冷却器11的半贫液从中间填料的上部加入。The lean liquid from the lean liquid cooler 7 is added from the upper part of the uppermost packing, and the semi-lean liquid from the semi-lean liquid cooler 11 is added from the upper part of the middle packing.
吸收塔1的底部排出的CO2富液进入闪蒸罐2进行初步减压解吸，闪蒸罐2顶部排出的解吸气体经过解吸气冷却器14进入气液分离器15；The CO2- rich liquid discharged from the bottom of the absorption tower 1 enters the flash tank 2 for preliminary decompression and desorption, and the desorbed gas discharged from the top of the flash tank 2 passes through the desorbed gas cooler 14 and enters the gas-liquid separator 15;
闪蒸罐2底部的排出液相分两路，一路经贫液换热器3预热后进入高压解吸塔4进行解吸，另一部经半贫液换热器8预热后进入低压解吸塔9进行解吸。The discharged liquid phase at the bottom of the flash tank 2 is divided into two paths, one path is preheated by the lean liquid heat exchanger 3 and enters the high-pressure desorption tower 4 for desorption, and the other path is preheated by the semi-lean liquid heat exchanger 8 and enters the low-pressure desorption tower 9 for desorption.
贫液换热器3通过高压解吸塔4塔釜的热贫液加热，半贫液换热器8通过低压解吸塔9塔釜的热半贫液加热。The lean liquid heat exchanger 3 is heated by the hot lean liquid in the bottom of the high-pressure desorption tower 4 , and the semi-lean liquid heat exchanger 8 is heated by the hot semi-lean liquid in the bottom of the low-pressure desorption tower 9 .
高压解吸塔4通过高压解吸再沸器5加热，高压解吸再沸器5热源采用来自界区外的蒸汽；高压解吸塔4底部的热贫液通过贫液换热器3回收余热后用贫液泵6送往贫液冷却器7进一步降温，之后送往吸收塔1循环使用。The high-pressure desorption tower 4 is heated by the high-pressure desorption reboiler 5, and the heat source of the high-pressure desorption reboiler 5 is steam from outside the boundary area; the hot lean liquid at the bottom of the high-pressure desorption tower 4 recovers the waste heat through the lean liquid heat exchanger 3 and is sent to the lean liquid cooler 7 by the lean liquid pump 6 for further cooling, and then sent to the absorption tower 1 for recycling.
高压解吸塔4塔顶的解吸气体进入低压解吸塔9下部的第二低压解吸再沸器13回收热量，并经解吸气冷却器14进一步冷凝后进入气液分离器15。The desorbed gas at the top of the high-pressure desorber 4 enters the second low-pressure desorber reboiler 13 at the bottom of the low-pressure desorber 9 to recover heat, and enters the gas-liquid separator 15 after further condensation by the desorbed gas cooler 14 .
低压解吸塔9有两个再沸器，其中第一低压解吸再沸器12由外来蒸汽提供热源，第二低压解吸再沸器13由来自高压解吸塔4顶部的解吸气提供热源。The low-pressure desorption tower 9 has two reboilers, wherein the first low-pressure desorption reboiler 12 is provided with a heat source by external steam, and the second low-pressure desorption reboiler 13 is provided with a heat source by the desorbed gas from the top of the high-pressure desorption tower 4.
低压解吸塔9底部的半贫液经半贫液换热器8换热，之后由半贫液泵10送入半贫液冷却器11进一步降温后返回吸收塔1循环使用。The semi-lean liquid at the bottom of the low-pressure desorption tower 9 is heat-exchanged in the semi-lean liquid heat exchanger 8, and then sent to the semi-lean liquid cooler 11 by the semi-lean liquid pump 10 for further cooling, and then returned to the absorption tower 1 for recycling.
低压解吸塔9塔顶的解吸气体经解吸气冷却器14进一步冷凝后进入气液分离器15。The desorbed gas at the top of the low-pressure desorber 9 is further condensed by the desorbed gas cooler 14 and then enters the gas-liquid separator 15 .
气液分离器15底部的冷凝液通过冷凝液泵16分别返回高压解吸塔4和低压解吸塔9；气液分离器15上部的气体出口为CO2产品气。The condensate at the bottom of the gas-liquid separator 15 is returned to the high-pressure desorption tower 4 and the low-pressure desorption tower 9 respectively through the condensate pump 16; the gas outlet at the top of the gas-liquid separator 15 is the CO2 product gas.
Claims (6)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910340516.3A CN109999618B (en) | 2019-04-25 | 2019-04-25 | System and method for separating carbon dioxide from medium-high pressure gas source |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910340516.3A CN109999618B (en) | 2019-04-25 | 2019-04-25 | System and method for separating carbon dioxide from medium-high pressure gas source |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109999618A CN109999618A (en) | 2019-07-12 |
| CN109999618B true CN109999618B (en) | 2024-05-14 |
Family
ID=67174287
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910340516.3A Active CN109999618B (en) | 2019-04-25 | 2019-04-25 | System and method for separating carbon dioxide from medium-high pressure gas source |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109999618B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110655959B (en) * | 2019-11-11 | 2024-05-14 | 新疆八一钢铁股份有限公司 | CO is removed to ouye stove gas2Device and method for controlling the same |
| CN114515497B (en) * | 2020-11-19 | 2023-06-06 | 中国石油化工股份有限公司 | Treatment system and treatment method for divinylbenzene production tail gas |
| CN112452109B (en) * | 2020-12-31 | 2021-08-27 | 双盾环境科技有限公司 | Desorption SO for improving desulfurization absorbent2Efficient process |
| CN114570164B (en) * | 2022-03-31 | 2022-12-30 | 四川益能康生环保科技有限公司 | CO 2 Or SO 2 Pressure swing regeneration energy-saving process for organic amine solution of trapping system |
| CN115920593B (en) * | 2022-11-25 | 2024-05-31 | 新疆敦华绿碳技术股份有限公司 | Absorption device based on double desorption units and production system |
| CN115779639A (en) * | 2022-11-25 | 2023-03-14 | 新疆敦华绿碳技术股份有限公司 | Carbon dioxide production system and control method |
| CN119236433B (en) * | 2024-10-25 | 2025-07-22 | 中石化节能技术服务有限公司 | Solvent regeneration system and method |
Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1176991A (en) * | 1996-08-28 | 1998-03-25 | 三菱重工业株式会社 | Process for removal and high-pressure recovery of carbon dioxide from high-pressure raw gas and system therefor |
| CN101643209A (en) * | 2009-07-14 | 2010-02-10 | 北京健坤伟华新能源科技有限公司 | Method for purifying and reclaiming carbon dioxide from landfill gas and device thereof |
| JP2011000525A (en) * | 2009-06-17 | 2011-01-06 | Mitsubishi Heavy Ind Ltd | Co2 recovering device and co2 recovering method |
| CN102133499A (en) * | 2011-03-03 | 2011-07-27 | 杨东 | System and method for trapping acid gas in smoke |
| CN102350177A (en) * | 2011-09-07 | 2012-02-15 | 航天环境工程有限公司 | Pneumatic trapping system and process for carbon dioxide (CO2) in smoke |
| CN102784546A (en) * | 2012-08-03 | 2012-11-21 | 中国华能集团清洁能源技术研究院有限公司 | An Efficient CO2 Capture System |
| CN102824815A (en) * | 2012-09-17 | 2012-12-19 | 江苏润丰环境工程有限公司 | Absorption extraction process for carbon dioxide in normal-pressure gas |
| CN102985161A (en) * | 2010-07-09 | 2013-03-20 | 美国碳捕集与利用技术开发公司 | A gas pressurized separation column and process to generate a high pressure product gas |
| CN103372365A (en) * | 2013-07-04 | 2013-10-30 | 天津大学 | Cement kiln waste heat power generation auxiliary carbon dioxide capture system device |
| CN103768895A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Method for low-energy consumption removal of carbon dioxide by hot potash |
| DE102013008852A1 (en) * | 2013-05-23 | 2014-11-27 | Linde Aktiengesellschaft | Process and apparatus for treating a sulfur-containing exhaust gas from a sulfur recovery |
| CN105268283A (en) * | 2015-09-28 | 2016-01-27 | 北京化工大学 | Combined absorption carbon dioxide trapping and compressing treatment technology |
| CN105664671A (en) * | 2016-03-17 | 2016-06-15 | 中石化南京工程有限公司 | Zero-carbon emission process gas purification method and device |
| CN106000000A (en) * | 2016-06-29 | 2016-10-12 | 中山大学 | Device and method for performing multistage flash, resolution and separation on synthetic ammonia decarburization absorption tower bottom pregnant solution |
| CN106362551A (en) * | 2016-11-23 | 2017-02-01 | 四川大学 | System and technology for trapping CO2 in smoke |
| CN107754568A (en) * | 2017-11-28 | 2018-03-06 | 沈建冲 | A kind of device and gas recovery process of low energy consumption flue gas trapping and recovering carbon dioxide |
| CN207562634U (en) * | 2017-11-23 | 2018-07-03 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN |
| CN108236831A (en) * | 2017-11-23 | 2018-07-03 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN |
| CN108815993A (en) * | 2018-07-24 | 2018-11-16 | 中石化石油工程技术服务有限公司 | The carbon dioxide capture system utilized based on Waste Heat Recovery |
| CN210410096U (en) * | 2019-04-25 | 2020-04-28 | 华能国际电力股份有限公司 | Separation system for carbon dioxide in medium-high pressure gas source |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101485956B1 (en) * | 2013-12-04 | 2015-01-26 | 한국에너지기술연구원 | System and Method for Separating and Collecting Acidic gas |
| JP2016215105A (en) * | 2015-05-18 | 2016-12-22 | 株式会社東芝 | Carbon dioxide recovery device and carbon dioxide recovery method |
| CN109529549A (en) * | 2017-09-22 | 2019-03-29 | 江苏新世纪江南环保股份有限公司 | Application of ultra-clean ammonia desulfurization technology to carbon capture process |
-
2019
- 2019-04-25 CN CN201910340516.3A patent/CN109999618B/en active Active
Patent Citations (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1176991A (en) * | 1996-08-28 | 1998-03-25 | 三菱重工业株式会社 | Process for removal and high-pressure recovery of carbon dioxide from high-pressure raw gas and system therefor |
| JP2011000525A (en) * | 2009-06-17 | 2011-01-06 | Mitsubishi Heavy Ind Ltd | Co2 recovering device and co2 recovering method |
| CN101643209A (en) * | 2009-07-14 | 2010-02-10 | 北京健坤伟华新能源科技有限公司 | Method for purifying and reclaiming carbon dioxide from landfill gas and device thereof |
| CN102985161A (en) * | 2010-07-09 | 2013-03-20 | 美国碳捕集与利用技术开发公司 | A gas pressurized separation column and process to generate a high pressure product gas |
| CN102133499A (en) * | 2011-03-03 | 2011-07-27 | 杨东 | System and method for trapping acid gas in smoke |
| CN102350177A (en) * | 2011-09-07 | 2012-02-15 | 航天环境工程有限公司 | Pneumatic trapping system and process for carbon dioxide (CO2) in smoke |
| CN102784546A (en) * | 2012-08-03 | 2012-11-21 | 中国华能集团清洁能源技术研究院有限公司 | An Efficient CO2 Capture System |
| CN102824815A (en) * | 2012-09-17 | 2012-12-19 | 江苏润丰环境工程有限公司 | Absorption extraction process for carbon dioxide in normal-pressure gas |
| CN103768895A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Method for low-energy consumption removal of carbon dioxide by hot potash |
| DE102013008852A1 (en) * | 2013-05-23 | 2014-11-27 | Linde Aktiengesellschaft | Process and apparatus for treating a sulfur-containing exhaust gas from a sulfur recovery |
| CN103372365A (en) * | 2013-07-04 | 2013-10-30 | 天津大学 | Cement kiln waste heat power generation auxiliary carbon dioxide capture system device |
| CN105268283A (en) * | 2015-09-28 | 2016-01-27 | 北京化工大学 | Combined absorption carbon dioxide trapping and compressing treatment technology |
| CN105664671A (en) * | 2016-03-17 | 2016-06-15 | 中石化南京工程有限公司 | Zero-carbon emission process gas purification method and device |
| CN106000000A (en) * | 2016-06-29 | 2016-10-12 | 中山大学 | Device and method for performing multistage flash, resolution and separation on synthetic ammonia decarburization absorption tower bottom pregnant solution |
| CN106362551A (en) * | 2016-11-23 | 2017-02-01 | 四川大学 | System and technology for trapping CO2 in smoke |
| CN207562634U (en) * | 2017-11-23 | 2018-07-03 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN |
| CN108236831A (en) * | 2017-11-23 | 2018-07-03 | 中石化石油工程技术服务有限公司 | Carbon dioxide capture system based on UTILIZATION OF VESIDUAL HEAT IN |
| CN107754568A (en) * | 2017-11-28 | 2018-03-06 | 沈建冲 | A kind of device and gas recovery process of low energy consumption flue gas trapping and recovering carbon dioxide |
| CN108815993A (en) * | 2018-07-24 | 2018-11-16 | 中石化石油工程技术服务有限公司 | The carbon dioxide capture system utilized based on Waste Heat Recovery |
| CN210410096U (en) * | 2019-04-25 | 2020-04-28 | 华能国际电力股份有限公司 | Separation system for carbon dioxide in medium-high pressure gas source |
Non-Patent Citations (2)
| Title |
|---|
| 热钾碱法脱碳溶液双塔变压再生改造及余热回收;魏有福;张静;;化肥设计;20131025(第05期);第49-51页 * |
| 燃煤电厂碳捕集系统节能潜力分析;冀树芳;王军;;现代化工;20151220(第12期);第160-163页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109999618A (en) | 2019-07-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN114768488B (en) | Coal-fired unit flue gas carbon dioxide entrapment system | |
| CA2670395C (en) | Improved absorbent regeneration | |
| CN102895860B (en) | Method and system for reducing consumption of chemical absorption CO2 capture process | |
| CN103463955B (en) | A kind of technique of separation and recovery carbon dioxide from industrial tail gas | |
| CN105749728B (en) | Method and apparatus for capturing carbon dioxide | |
| CN102225297B (en) | Heat pump regeneration process for desulphurization solvent used in flue gas desulphurization by solvent cyclic absorption method | |
| CN106362551A (en) | System and technology for trapping CO2 in smoke | |
| CN102784546A (en) | An Efficient CO2 Capture System | |
| CN114963218A (en) | Flue gas waste heat recovery device and method coupled with carbon capture | |
| CN107715650B (en) | A carbon capture system regeneration gas heat recovery structure | |
| CN102895843A (en) | System for recycling waste heat produced by methyl-diethanolamine (MDEA) decarburization process by using ultra high temperature heat pump | |
| CN111298604A (en) | System and method for capturing carbon dioxide in flue gas | |
| CN115463521A (en) | Low-energy-consumption carbon capture device and method | |
| CN118767623A (en) | Carbon dioxide capture system and method | |
| CN114632402B (en) | Trapping method of flue gas carbon dioxide trapping system | |
| CN221771923U (en) | A carbon capture system with integrated heat pump | |
| CN217795387U (en) | Low-energy-consumption carbon trapping device | |
| CN217220919U (en) | CO 2 And N 2 Composite trapping and purifying system | |
| CN217410286U (en) | A flue gas deep carbon capture device for recovering waste heat | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source | |
| CN105251316B (en) | The direct thermodynamic-driven of independent solar utilizes mixed working fluid removing CO2System | |
| CN117180928A (en) | Gas trapping and storing system and method | |
| CN205481906U (en) | System for utilize mixed working medium to pass through heating power driven compact desorption carbon dioxide | |
| CN117919895A (en) | Low-cost low-concentration CO2Trapping system and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 100031, 6, Fuxing Avenue, Xicheng District, Beijing Applicant after: Huaneng Power International,Inc. Applicant after: HUANENG CLEAN ENERGY Research Institute Address before: 100031 Beijing city Xicheng District Fuxingmen South Street No. 2 C Applicant before: Huaneng Power International,Inc. Applicant before: HUANENG CLEAN ENERGY Research Institute |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |