CN104958998A - 一种富液自驱动萃取分相和撕裂再生的co2捕集系统 - Google Patents
一种富液自驱动萃取分相和撕裂再生的co2捕集系统 Download PDFInfo
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- CN104958998A CN104958998A CN201510388809.0A CN201510388809A CN104958998A CN 104958998 A CN104958998 A CN 104958998A CN 201510388809 A CN201510388809 A CN 201510388809A CN 104958998 A CN104958998 A CN 104958998A
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- 238000011069 regeneration method Methods 0.000 title claims abstract description 27
- 230000008929 regeneration Effects 0.000 title claims abstract description 22
- 238000000605 extraction Methods 0.000 title claims abstract description 10
- 210000001138 Tears Anatomy 0.000 title claims abstract description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound 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- UIIMBOGNXHQVGW-UHFFFAOYSA-M NaHCO3 Chemical compound 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[Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000005712 crystallization Effects 0.000 description 3
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound 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[K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 3
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- 238000003795 desorption Methods 0.000 description 2
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- 239000005431 greenhouse gas Substances 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 235000015320 potassium carbonate Nutrition 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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Classifications
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
一种富液自驱动萃取分相和撕裂再生的CO2捕集系统，吸收塔底部CO2富液出口通过富液泵与分相澄清器的料液导流管相连；分相澄清器的轻相收集室出口分两路一路与混合罐相连，另一路经阀门、溶液净化器与混合罐相连；重相收集室通过富相泵、贫富换热器与再生塔相连；再生塔底部的贫液出口通过贫液泵、贫富换热器与混合罐相连；混合罐的底部溶液出口通过吸收液泵与吸收塔的吸收液相连；再生塔顶部的CO2再生气出口通过冷却器与气液分离罐相连；再沸器设置在再生塔底部或内部；本发明通过CO2富液自驱动萃取分层为液-液两相，实现负载CO2的组分在富相中的浓缩和再分配，从而减少CO2再生过程中的富液量和水的参与度，较大程度的降低CO2再生能耗和捕集成本。
Description
技术领域
[0001] 本发明属于工艺气体净化、二氧化碳减排等技术领域，具体涉及一种富液自驱动萃取分相和撕裂再生的CO2捕集系统。
背景技术
[0002] 二氧化碳(CO2)是导致全球气候变暖的主要温室气体，CO2的捕集、利用及封存已成为国际社会关注的热点课题之一。我国燃煤发电CO2排放量约占工业总排放量的50%，燃煤电厂烟气中CO2的捕集分离是温室气体减排的重要领域。此外，炼钢、水泥、化工(如合成氨、制氢、天然气净化)等工业领域也存在大量CO2捕集或分离过程。捕集或分离CO 2的方法主要有吸收法、吸附法、膜分离、低温分离等，其中吸收法是目前最为成熟和有望实现大规模商业化应用的0)2捕集分离技术。
[0003] 传统的CO2吸收法捕集分离技术在应用过程中的能耗和运行成本较高。吸收CO 2后的富液全部进入再生塔解吸，且富液中水的比例较高(一般70%以上)，这不仅增加了再生时的富液量，而且水大量挥发也导致额外的能耗，从而使得系统整体能耗增大。吸收剂再生所消耗的蒸汽热能在整个系统能耗中占到了绝大比重。因此，降低再生富液量，减少富液的水含量，将可以有效的降低0)2再生能耗和捕集成本。
[0004] 基于碳酸钾溶液的稠浆型CO2捕集工艺，是利用碳酸钾和碳酸氢钾在水中的溶解度差异，采用强制冷却或蒸发的方式使得富液过饱和而析出碳酸氢钾结晶，之后加热解吸碳酸氢钾晶浆液。该工艺中，吸收的CO2以碳酸氢钾结晶的形式析出，晶浆解吸大幅降低了再生时水的参与度和再生能耗。但该工艺需要强制冷却或者蒸发结晶，也额外增加了一部分公用工程量，而且结晶颗粒也可能导致管道堵塞等一些工程问题。
[0005] 为进一步降低公用工程量，我们研宄开发了一种吸收0)2后富液能够自动萃取分层为液-液两相的CO2吸收剂，其中CO 2在富相的再分配率达98%以上，贫相几乎不含CO 2。富液分相浓缩过程无需冷却或升温蒸发，并且不会出现固体结晶物，降低了工艺操作难度。浓缩后的CO2富相进入再生塔进行解吸，减少了再生时的富液量，达到节能降耗的目的，而且工艺过程也易于实现吸收剂的在线纯化处理。
发明内容
[0006] 为了克服现有技术的缺陷，本发明的目的在于提供一种富液自驱动萃取分相和撕裂再生的CO2捕集系统，该系统可以实现富液自动萃取分层为液-液两相和CO2富相的单独再生，减少了进入再生塔的总液量，达到节能降耗的目的。
[0007] 为达到上述目的，本发明采用的技术方案是:
[0008] 一种富液自驱动萃取分相和撕裂再生的0)2捕集系统，包括吸收塔1，吸收塔I由底部的吸收段1-1、中部的洗涤段1-2和顶部的除沫段1-3组成，吸收塔I的底部0)2富液出口通过富液泵2与分相澄清器3的料液入口相连；分相澄清器3由料液导流管3-1、分相澄清室3-2、轻相收集室3-3和重相收集室3-4组成；轻相收集室3-3的出口分两路，一路直接与混合罐4的入口相连，另一路通过阀门5、溶液净化器6与混合罐4的入口相连；重相收集室3-4的出口通过富相泵7、贫富换热器8与再生塔9的入口相连；再生塔9底部的贫液出口通过贫液泵10、贫富换热器8与混合罐4的入口相连；混合罐4的底部溶液出口通过吸收液泵11与吸收段1-1上端的吸收液入口相连；再生塔9顶部的CO2再生气出口通过冷却器12与气液分离罐13的入口相连；与再生塔9配套的再沸器14设置在装置底部或内部。
[0009] 所述的分相澄清器3由料液导流管3-1、分相澄清室3-2、轻相收集室3_3和重相收集室3-4组成，料液导流管3-1设置于分相澄清器3的一侧上方，轻相收集室3-3和重相收集室3-4的入口设置于整个分相澄清器3的中上部，并分别通过轻相堰、重相堰与分相澄清室3-2隔开。
[0010] 由于本发明设计有分相澄清器3，因此通过0)2富液自驱动萃取可以分层为液-液两相，能够实现负载CO2的组分在富相中的浓缩和再分配，并输送至再生塔进行热再生，不含CO2的贫相不参与热再生，从而降低CO2再生过程中的富液量和水的参与度，达到节能降耗的目的。
附图说明
[0011] 附图为本发明的结构示意图。
具体实施方式
[0012] 下面结合附图对本发明作进一步的详细说明。
[0013] 参见附图，一种富液自驱动萃取分相和撕裂再生的0)2捕集系统，包括吸收塔1，吸收塔I由底部的吸收段1-1、中部的洗涤段1-2和顶部的除沫段1-3组成，吸收塔I的底部CO2富液出口通过富液泵2与分相澄清器3的料液入口相连；分相澄清器3由料液导流管3-1、分相澄清室3-2、轻相收集室3-3和重相收集室3-4组成；轻相收集室3_3的出口分两路，一路直接与混合罐4的入口相连，另一路通过阀门5、溶液净化器6与混合罐4的入口相连；重相收集室3-4的出口通过富相泵7、贫富换热器8与再生塔9的入口相连；再生塔9底部的贫液出口通过贫液泵10、贫富换热器8与混合罐4的入口相连；混合罐4的底部溶液出口通过吸收液泵11与吸收段1-1上端的吸收液入口相连；再生塔9顶部的CO2再生气出口通过冷却器12与气液分离罐13的入口相连；与再生塔9配套的再沸器14设置在装置底部或内部。
[0014] 所述的分相澄清器3由料液导流管3-1、分相澄清室3-2、轻相收集室3_3和重相收集室3-4组成，料液导流管3-1设置于分相澄清器3的一侧上方，轻相收集室3-3和重相收集室3-4的入口设置于整个分相澄清器3的中上部，并分别通过轻相堰、重相堰与分相澄清室3-2隔开。
[0015] 本发明的工作原理如下:
[0016] 含有0)2混合气由吸收塔I下部的气体进口输入吸收塔I内，与此同时来自混合罐4的吸收溶液由吸收段1-1上端的吸收溶液入口向塔内喷淋，CO2气体与吸收剂在塔内充分逆向接触而被吸收剂吸收。被吸收剂脱除0)2后的气体继续向上流动，通过洗涤段1-2和除沫段1-3后经吸收塔I顶部的气体出口直接排入大气。吸收CO2后的富液在吸收塔I底部通过富液泵2进入分相澄清器3的料液导流管3-1，之后在分相澄清室3-2内自动萃取分相实现CO2的再分配，不含CO 2的贫相进入轻相收集室3-3，富含CO 2的富相进入重相收集室3-4ο来自轻相收集室3-3的贫相分两路，一路直接进入混合罐4，一路经过阀门5、溶液净化器6进入混合罐。溶液净化器6通过吸附或离子交换技术除去溶液中积累的杂质离子，达到纯化吸收溶剂的目的。来自重相收集室3-4的富相由富相泵7送至贫富换热器8，与来自再生塔9底部的热贫液换热升温后进入再生塔9进行热解吸。再沸器14提供富液再生所需的热量。含有部分水蒸气、吸收剂蒸气的0)2再生气由再生塔9顶部的气体出口流出，经过冷却器12冷却和气液分离罐13后成为高浓度CO2产品气，冷凝液返回再生塔9。脱除CO2后的贫液从再生塔9底部由贫液泵10引出，经过贫富换热器8换热后进入混合罐4，与来自分相澄清器3的贫相进行混合形成吸收溶液。吸收溶液由吸收液泵11送至吸收段1-1的上端吸收液入口而循环使用。
Claims (2)
1.一种富液自驱动萃取分相和撕裂再生的CO 2捕集系统，包括吸收塔(I)，其特征在于，吸收塔(I)由底部的吸收段(1-1)、中部的洗涤段(1-2)和顶部的除沫段(1-3)组成；吸收塔(I)的底部CO2富液出口通过富液泵(2)与分相澄清器(3)的料液入口相连；分相澄清器(3)主要由料液导流管(3-1)、分相澄清室(3-2)、轻相收集室(3-3)和重相收集室(3-4)组成；轻相收集室(3-3)的出口分两路，一路直接与混合罐(4)的入口相连，一路通过阀门(5)、溶液净化器(6)与混合罐(4)的入口相连；重相收集室(3-4)的出口通过富相泵(7)、贫富换热器(8)与再生塔(9)的入口相连；再生塔(9)底部的贫液出口通过贫液泵(10)、贫富换热器(8)与混合罐(4)的入口相连；混合罐(4)的底部溶液出口通过吸收液泵(11)与吸收段(1-1)上端的吸收液入口相连；再生塔(9)顶部的CO2再生气出口通过冷却器(12)与气液分离罐(13)的入口相连；与再生塔(9)配套的再沸器(14)设置在装置底部或内部。
2.根据权利要求1所述的分相澄清器(3)，其特征在于，分相澄清器(3)由料液导流管(3-1)、分相澄清室(3-2)、轻相收集室(3-3)和重相收集室(3-4)组成，料液导流管(3_1)设置于分相澄清器⑶的一侧上方，轻相收集室(3-3)和重相收集室(3-4)的入口设置于整个分相澄清器(3)的中上部，并分别通过轻相堰、重相堰与分相澄清室(3-2)隔开。
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