CN106000009B - A kind of double-tower type MEDA handles landfill gas system - Google Patents
A kind of double-tower type MEDA handles landfill gas system Download PDFInfo
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- CN106000009B CN106000009B CN201610571782.3A CN201610571782A CN106000009B CN 106000009 B CN106000009 B CN 106000009B CN 201610571782 A CN201610571782 A CN 201610571782A CN 106000009 B CN106000009 B CN 106000009B
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- 241000948268 Meda Species 0.000 title claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 148
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 64
- 238000010521 absorption reaction Methods 0.000 claims abstract description 44
- 239000002253 acid Substances 0.000 claims abstract description 42
- 238000005406 washing Methods 0.000 claims abstract description 30
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000000498 cooling water Substances 0.000 claims abstract description 19
- 238000010992 reflux Methods 0.000 claims abstract description 19
- 239000012190 activator Substances 0.000 claims abstract description 12
- 239000002994 raw material Substances 0.000 claims abstract description 8
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 claims abstract 4
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims abstract 4
- 230000008676 import Effects 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims 3
- 230000007423 decrease Effects 0.000 claims 1
- 239000012530 fluid Substances 0.000 claims 1
- 238000009738 saturating Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 83
- 230000008929 regeneration Effects 0.000 abstract description 40
- 238000011069 regeneration method Methods 0.000 abstract description 40
- 238000011084 recovery Methods 0.000 abstract description 14
- 238000000746 purification Methods 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 231100001261 hazardous Toxicity 0.000 abstract description 2
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 20
- 238000000034 method Methods 0.000 description 13
- 238000001816 cooling Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000014509 gene expression Effects 0.000 description 1
- WABPQHHGFIMREM-UHFFFAOYSA-N lead(0) Chemical compound [Pb] WABPQHHGFIMREM-UHFFFAOYSA-N 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- 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
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- 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
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- 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
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/60—Additives
- B01D2252/602—Activators, promoting agents, catalytic agents or enzymes
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- 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
一种双塔式MEDA处理填埋气系统属于环境工程保护和气体提纯处理技术领域，尤其涉及一种双塔式MEDA处理填埋气系统。本发明提供一种可以有效处理填埋气体中的CO2和H2S等其中的危害气体的双塔式MEDA处理填埋气系统。本发明包括原料气箱、原料气增压泵、吸收塔、套管式微反应器、活化剂哌嗪入口、气液分离器、液力透平、循环泵、闪蒸器、贫富液换热器、半贫液换热器、再生塔、再沸器、冷却水箱、热泵、分离器、酸水回流泵、酸气回收箱、半贫液后冷器、贫液后冷器、MDEA循环泵、洗涤槽回流泵、水洗涤槽、处理气收集箱，其结构要点套管式微反应器设置在吸收塔内一侧的腔体内。
A double-tower MEDA landfill gas treatment system belongs to the technical field of environmental engineering protection and gas purification treatment, and in particular relates to a double-tower MEDA landfill gas treatment system. The invention provides a double-tower MEDA landfill gas treatment system that can effectively treat CO 2 and H 2 S and other hazardous gases in the landfill gas. The invention includes a raw material gas tank, a raw material gas booster pump, an absorption tower, a casing microreactor, an activator piperazine inlet, a gas-liquid separator, a hydraulic turbine, a circulating pump, a flash evaporator, and a lean-rich liquid heat exchanger , semi-lean liquid heat exchanger, regeneration tower, reboiler, cooling water tank, heat pump, separator, acid water reflux pump, acid gas recovery tank, semi-lean liquid aftercooler, lean liquid aftercooler, MDEA circulation pump, The washing tank reflux pump, the water washing tank, and the treated gas collection box have structural points that the sleeve-type micro-reactor is arranged in the cavity on one side of the absorption tower.
Description
技术领域technical field
本发明属于环境工程保护和气体提纯处理技术领域，尤其涉及一种双塔式MEDA处理填埋气系统。The invention belongs to the technical field of environmental engineering protection and gas purification treatment, and in particular relates to a double-tower MEDA system for treating landfill gas.
背景技术Background technique
溶剂吸收法捕集CO2和H2S是目前应用最为广泛的方法，以甲基二乙醇胺（MDEA）为吸收液，在MDEA 中添加活化剂哌嗪可以有效提高其吸收能力。MEDA相比其他的吸收液再生容易、能耗低，MEDA蒸汽压底，吸收酸性气体溶剂损失少，溶剂对CO2和H2S负载量大，净化度高，是一种化学法净化的高效低能耗的酸性气体脱除剂。但是对于单一的吸收CO2或H2S，MDEA的去除效率会很高，尤其对CO2会达到95%以上。Solvent absorption method is currently the most widely used method to capture CO 2 and H 2 S. Using methyldiethanolamine (MDEA) as the absorption liquid, adding activator piperazine to MDEA can effectively improve its absorption capacity. Compared with other absorption liquids, MEDA is easy to regenerate and has low energy consumption. MEDA has a vapor pressure bottom, absorbs less acid gas solvent loss, has a large load of CO 2 and H 2 S by the solvent, and has a high degree of purification. It is an efficient chemical purification method. Low energy consumption acid gas remover. But for the single absorption of CO 2 or H 2 S, the removal efficiency of MDEA will be very high, especially for CO 2 will reach more than 95%.
那么问题就在MDEA与H2S、CO2的反应差异存在差异，造成MDEA溶液吸收H2S和CO2的速率不同，从而使得MDEA能够在含有H2S和CO2的体系中选择性吸收H2S。因此，努力改善加快CO2的速率是使得MDEA溶液同时吸收CO2和H2S是关键。Then the problem is that there are differences in the reaction differences between MDEA and H 2 S and CO 2 , which cause the MDEA solution to absorb H 2 S and CO 2 at different rates, so that MDEA can selectively absorb in systems containing H 2 S and CO 2 H2S . Therefore, efforts to improve and accelerate the rate of CO 2 is the key to make MDEA solution absorb CO 2 and H 2 S simultaneously.
发明内容Contents of the invention
本发明就是针对上述问题，提供一种可以有效处理填埋气体中的CO2和H2S等其中的危害气体的双塔式MEDA处理填埋气系统。The present invention aims at the above problems and provides a double-tower MEDA landfill gas treatment system that can effectively treat CO 2 and H 2 S and other hazardous gases in the landfill gas.
为实现上述目的，本发明采用如下技术方案，本发明包括原料气箱、原料气增压泵、吸收塔、套管式微反应器、活化剂哌嗪入口、气液分离器、液力透平、循环泵、闪蒸器、贫富液换热器、半贫液换热器、再生塔、再沸器、冷却水箱、热泵、分离器、酸水回流泵、酸气回收箱、半贫液后冷器、贫液后冷器、MDEA循环泵、洗涤槽回流泵、水洗涤槽、处理气收集箱，其结构要点套管式微反应器设置在吸收塔内一侧的腔体内，活化剂哌嗪入口与套管式微反应器外侧腔体连通设置在腔体下部，套管式微反应器下端进口通过原料气增压泵与原料气箱相连。In order to achieve the above object, the present invention adopts the following technical scheme, the present invention comprises feed gas tank, feed gas booster pump, absorption tower, casing microreactor, activator piperazine inlet, gas-liquid separator, hydraulic turbine, Circulation pump, flash evaporator, lean-rich liquid heat exchanger, semi-lean liquid heat exchanger, regeneration tower, reboiler, cooling water tank, heat pump, separator, acid water reflux pump, acid gas recovery tank, semi-lean liquid aftercooling device, lean liquid aftercooler, MDEA circulating pump, washing tank reflux pump, water washing tank, treated gas collection box, the structural points of the sleeve-type microreactor are set in the cavity on one side of the absorption tower, and the inlet of the activator piperazine It communicates with the outer cavity of the sleeve-type micro-reactor and is arranged at the lower part of the cavity, and the inlet at the lower end of the sleeve-type micro-reactor is connected with the feed gas box through a feed gas booster pump.
套管式微反应器上端出口上方的腔体上端设置有竖向出口，竖向出口与吸收塔内上端的气液分离器入口相连，气液分离器上端气体出口与水洗涤槽相连，水洗涤槽的气体出口与处理气收集箱相连，水洗涤槽的液体出口通过洗涤槽回流泵与竖向再生塔的中部进口相连；气液分离器远离腔体侧下端设置有向下的液体出口，液体出口与腔体外吸收塔内空间连通，吸收塔下端设置有与腔体外吸收塔内空间连通的横向富液出口，富液出口与液力透平的进口相连，液力透平的出口通过闪蒸器分别与贫富液换热器、半贫液换热器的第一换热通道入口相连，贫富液换热器、半贫液换热器的第一换热通道出口与再沸器的富液进口相连。The upper end of the cavity above the upper outlet of the casing microreactor is provided with a vertical outlet, the vertical outlet is connected to the inlet of the gas-liquid separator at the upper end of the absorption tower, the gas outlet at the upper end of the gas-liquid separator is connected to the water washing tank, and the water washing tank The gas outlet of the gas-liquid separator is connected to the processing gas collection box, and the liquid outlet of the water washing tank is connected to the middle inlet of the vertical regeneration tower through the washing tank reflux pump; It communicates with the inner space of the absorption tower outside the chamber, and the lower end of the absorption tower is provided with a horizontal rich liquid outlet that communicates with the inner space of the absorption tower outside the chamber. The rich liquid outlet is connected with the inlet of the hydraulic turbine, and the outlet of the hydraulic turbine is separated by It is connected with the inlet of the first heat exchange channel of the lean-rich liquid heat exchanger and the semi-lean liquid heat exchanger, and the outlet of the first heat exchange channel of the lean-rich liquid heat exchanger and the semi-lean liquid heat exchanger is connected with the rich liquid of the reboiler The import is connected.
液力透平的驱动输出端与循环泵的驱动输入端相连，循环泵的出口同与套管式微反应器外侧腔体连通设置在腔体下部的半贫液进口相连，循环泵的进口通过半贫液后冷器与半贫液换热器的第二换热通道出口相连，半贫液换热器的第二换热通道入口与再生塔中部半贫液出口相连。The driving output end of the hydraulic turbine is connected with the driving input end of the circulating pump, the outlet of the circulating pump is connected with the semi-poor liquid inlet which is connected with the outer cavity of the casing microreactor and arranged at the lower part of the cavity, and the inlet of the circulating pump passes through the semi-lean liquid inlet. The lean liquid aftercooler is connected to the outlet of the second heat exchange channel of the semi-lean liquid heat exchanger, and the inlet of the second heat exchange channel of the semi-lean liquid heat exchanger is connected to the semi-lean liquid outlet in the middle of the regeneration tower.
贫富液换热器的第二换热通道入口与再生塔下端贫液出口相连，贫富液换热器的第二换热通道出口依次通过贫液后冷器、MDEA循环泵同与套管式微反应器外侧腔体连通设置在腔体上部的贫液进口相连。The inlet of the second heat exchange channel of the lean-rich liquid heat exchanger is connected with the lean liquid outlet at the lower end of the regeneration tower, and the outlet of the second heat exchange channel of the lean-rich liquid heat exchanger passes through the lean liquid aftercooler, MDEA circulating pump and casing in sequence The outer cavity of the microreactor is connected to the poor liquid inlet provided on the upper part of the cavity.
再沸器的气体出口与再生塔下部的气体入口相连，再沸器的半贫液出口与再生塔下部的液体入口相连；再生塔下端的半贫液出口分别与再沸器的半贫液入口、热泵半贫液加热口相连。The gas outlet of the reboiler is connected with the gas inlet at the lower part of the regeneration tower, and the semi-lean liquid outlet of the reboiler is connected with the liquid inlet at the lower part of the regeneration tower; the semi-lean liquid outlet at the lower end of the regeneration tower is respectively connected with the semi-lean liquid inlet of the reboiler , The semi-lean liquid heating port of the heat pump is connected.
再沸器的冷凝水出口与冷却水箱的冷凝水入口相连，冷却水箱的冷凝水出口与热泵的换热液体进口相连，热泵的换热液体出口与冷却水箱的换热后冷凝水入口相连；热泵的换热气体入口与再生塔上端的热的酸水气出口相连，热泵的换热后出口与分离器的入口相连，分离器的酸气出口与酸气回收箱相连，分离器的酸水出口通过酸水回流泵与再生塔上端的酸水回流口相连。The condensed water outlet of the reboiler is connected with the condensed water inlet of the cooling water tank, the condensed water outlet of the cooling water tank is connected with the heat exchange liquid inlet of the heat pump, the heat exchange liquid outlet of the heat pump is connected with the condensed water inlet after heat exchange of the cooling water tank; the heat pump The heat exchange gas inlet of the heat pump is connected with the hot acid water gas outlet at the upper end of the regeneration tower, the heat exchange outlet of the heat pump is connected with the inlet of the separator, the acid gas outlet of the separator is connected with the acid gas recovery tank, and the acid water outlet of the separator The sour water reflux pump is connected to the sour water reflux port at the upper end of the regeneration tower.
作为一种优选方案，本发明所述半贫液后冷器与半贫液换热器的第二换热通道出口之间设置有阀门。As a preferred solution, a valve is provided between the semi-lean liquid aftercooler and the outlet of the second heat exchange channel of the semi-lean liquid heat exchanger in the present invention.
作为另一种优选方案，本发明所述贫富液换热器的第二换热通道入口与再生塔下端贫液出口之间设置有阀门。As another preferred solution, a valve is provided between the inlet of the second heat exchange channel of the lean-rich liquid heat exchanger and the lean liquid outlet at the lower end of the regeneration tower.
其次，本发明所述MDEA循环泵与贫液进口之间设置有阀门。Secondly, a valve is provided between the MDEA circulating pump and the lean liquid inlet in the present invention.
另外，本发明所述闪蒸器顶端闪蒸气出口与再生塔或酸气回收箱相连。In addition, the outlet of the flash gas at the top of the flash evaporator of the present invention is connected with the regeneration tower or the acid gas recovery tank.
本发明有益效果。The invention has beneficial effects.
本发明添加了液力透平装置可以利用富液的液体压力转化为循环泵的机械能。添加了热泵回收再生塔酸水的热能提供再沸器加热装置。添加了套管式微反应器协调CO2和H2S的吸收，使得吸收效率的最大化。最大的特点可以利用半贫液回流进吸收塔，减少再沸器部分重新加热。最后添加了吸收塔湿气的水槽洗涤进一步吸收可以溶于水的有害气体。该流程装置可以做到几乎没有污染，能源最大化的重新利用，且可以同时做到CO2和H2S最大化协调吸收等优点。The invention adds a hydraulic turbine device, which can convert the liquid pressure of the rich liquid into the mechanical energy of the circulating pump. A heat pump is added to recover the heat energy of the sour water in the regeneration tower to provide the reboiler heating device. A sleeve-type microreactor is added to coordinate the absorption of CO 2 and H 2 S, maximizing the absorption efficiency. The biggest feature is that the semi-lean liquid can be used to reflux into the absorption tower, reducing the reheating of the reboiler part. Finally, the water tank washing with the moisture of the absorption tower is added to further absorb the harmful gases that can be dissolved in water. The process device can achieve almost no pollution, maximize the reuse of energy, and can simultaneously achieve the advantages of maximizing the coordinated absorption of CO 2 and H 2 S.
一般认为MEDA去除CO2的效率高达95%以上，如果同时处理H2S,则去除H2S的效率会很低。这是因为反应时的速率的不一样，MEDA与CO2反应时偏慢而与H2S则偏快。所以采用一种套管式微反应器和活化剂哌嗪则可以加快MEDA与CO2反应让其与H2S的反应达到同步。在能源回收方面采用液力透平和热泵回收液体的压力给循环泵供给机械能和热泵回收酸水的热能供给再沸的半贫液。以及又增设了贫富/半贫富液换热器可以与MDEA富液进行换热回收热能。设置两个后制冷器分别为半贫/贫液后冷器。迅速的降低贫/半贫液换热后的余温，保证了达到吸收塔内部反应的条件。防止再生塔内部的温度对MDEA转贫的影响。采用再沸器，再生塔底部的半贫液进入再沸器，再沸后的半贫液和再沸器上部蒸汽又重回到再生塔。再沸器所产生的凝结水可直接输送到冷却水箱，这样可以充分利用和节约水资源。It is generally believed that the efficiency of CO 2 removal by MEDA is as high as 95%. If H 2 S is treated at the same time, the efficiency of removing H 2 S will be very low. This is because the reaction rate is different, MEDA reacts slowly with CO 2 and relatively fast with H 2 S. Therefore, the use of a casing microreactor and the activator piperazine can speed up the reaction of MEDA and CO 2 to synchronize the reaction with H 2 S. In terms of energy recovery, the hydraulic turbine and heat pump are used to recover the pressure of the liquid to supply the mechanical energy to the circulation pump, and the heat energy recovered by the heat pump to recover the acid water is used to supply the reboiled semi-lean liquid. And a rich-poor/semi-poor rich liquid heat exchanger is added to exchange heat with MDEA rich liquid to recover heat energy. The two aftercoolers are set as semi-lean/lean liquid aftercoolers respectively. The residual temperature after the heat exchange of the lean/semi-poor liquid is rapidly reduced to ensure the conditions for internal reaction of the absorption tower. Prevent the temperature inside the regeneration tower from affecting the leaning of MDEA. Using a reboiler, the semi-lean liquid at the bottom of the regeneration tower enters the reboiler, and the reboiled semi-lean liquid and steam from the upper part of the reboiler return to the regeneration tower. The condensed water produced by the reboiler can be directly sent to the cooling water tank, which can make full use of and save water resources.
一般认为凝结水是比较干净和清洁的。在再生塔的上部出来酸水气经过热泵后用分离器进行气液分离，酸水通过酸水回流泵回收进入再生塔，酸气用酸气回收箱进行回收。在吸收塔出来的净化气经过水洗涤槽，H2S溶于水和CO2微溶于水可以把未及时吸收的有害气体重新得到水洗，水洗后可直接接再生塔进行进一步的处理。在此工艺中大部分采用泵输送进行一步步气体净化处理。Condensate is generally considered to be relatively clean and clean. The acid water gas coming out of the upper part of the regeneration tower passes through the heat pump, and then the gas-liquid separation is carried out by the separator. The acid water is recovered into the regeneration tower through the acid water reflux pump, and the acid gas is recovered by the acid gas recovery box. The purified gas from the absorption tower passes through the water washing tank, where H 2 S is dissolved in water and CO 2 is slightly dissolved in water, so that the harmful gas that has not been absorbed in time can be washed again. After washing, it can be directly connected to the regeneration tower for further treatment. In this process, most of the pumps are used for step-by-step gas purification.
本发明中加入一个套管式微反应器和添加活化剂哌嗪加快MDEA与CO2的反应，这样可以满足MDEA与H2S与CO2的协调吸收。还有传统的双塔式处理填埋气是不经济的，例如从吸收塔出来的富液是经过加压的，为了不浪费能源考虑到回收液体压力因此添加进液力透平装置回收可以给循环泵供能用来半贫液的循环进入吸收塔。此工艺中加入半贫液与贫液两条冷却线进入吸收塔，减少半贫液经再沸器重新再沸过程节约能源。In the present invention, a jacketed microreactor and an activator piperazine are added to accelerate the reaction of MDEA and CO 2 , which can satisfy the coordinated absorption of MDEA, H 2 S and CO 2 . In addition, the traditional double-tower treatment of landfill gas is not economical. For example, the rich liquid from the absorption tower is pressurized. In order not to waste energy, it is considered to recover the liquid pressure, so it can be added to the hydraulic turbine for recovery. The circulation pump is used to circulate the semi-lean liquid into the absorption tower. In this process, two cooling lines of semi-lean liquid and lean liquid are added into the absorption tower to reduce the reboiling process of semi-lean liquid through the reboiler and save energy.
在回收酸气的热能时采用热泵把冷却水和酸气的热能换热再把换热后的热能接再沸器供给半贫液的再沸。酸气的凝结水经过热泵后经过分离器酸气排出收集，酸水回流进再生塔。为了吸收塔不能高效的吸收CO2和H2S，让湿的净化气体经过水洗涤槽进行洗涤，洗涤后洗涤液再回到再生塔让CO2和H2S析出。整个装置工艺以加快吸收塔吸收CO2和高效利用液压热能为主，可以大大降低净化工艺的成本。关键整工艺不会产生二次污染，保护了环境，去除CO2和H2S的效率等优点。When recovering the heat energy of the acid gas, the heat pump is used to exchange the heat energy of the cooling water and the acid gas, and then the heat energy after the heat exchange is connected to the reboiler to supply the reboil of the semi-lean liquid. The condensed water of the acid gas passes through the heat pump, and then the acid gas is discharged and collected through the separator, and the acid water flows back into the regeneration tower. In order that the absorption tower cannot efficiently absorb CO 2 and H 2 S, the wet purified gas is washed through a water washing tank, and the washing liquid is returned to the regeneration tower after washing to allow CO 2 and H 2 S to be precipitated. The entire device process is mainly based on accelerating the absorption of CO2 in the absorption tower and efficient use of hydraulic heat energy, which can greatly reduce the cost of the purification process. The key whole process does not produce secondary pollution, protects the environment, and has the advantages of high efficiency in removing CO 2 and H 2 S.
附图说明Description of drawings
下面结合附图和具体实施方式对本发明做进一步说明。本发明保护范围不仅局限于以下内容的表述。The present invention will be further described below in conjunction with the accompanying drawings and specific embodiments. The scope of protection of the present invention is not limited to the following expressions.
图1是本发明结构示意图。Fig. 1 is a schematic diagram of the structure of the present invention.
图中，1为原料气箱、2为原料气增压泵、3为吸收塔、4为套管式微反应器、5为活化剂哌嗪入口、6为气液分离器、7为液力透平、8为循环泵、9为闪蒸器、10为贫富液换热器、11为半贫液换热器、12为再生塔、13为再沸器、14为冷却水箱、15为热泵、16为分离器、17为酸水回流泵、18为酸气回收箱、19为半贫液后冷气、20为贫液后冷器、21为MDEA循环泵、22为洗涤槽回流泵、23为水洗涤槽、24为处理气收集箱。In the figure, 1 is the raw material gas tank, 2 is the raw material gas booster pump, 3 is the absorption tower, 4 is the casing microreactor, 5 is the inlet of the activator piperazine, 6 is the gas-liquid separator, and 7 is the hydraulic permeability Ping, 8 is circulation pump, 9 is flash evaporator, 10 is lean-rich liquid heat exchanger, 11 is semi-lean liquid heat exchanger, 12 is regeneration tower, 13 is reboiler, 14 is cooling water tank, 15 is heat pump, 16 is a separator, 17 is an acid water reflux pump, 18 is an acid gas recovery tank, 19 is a semi-lean liquid aftercooler, 20 is a lean liquid aftercooler, 21 is an MDEA circulation pump, 22 is a washing tank reflux pump, and 23 is The water washing tank, 24 is a processing gas collection box.
具体实施方式Detailed ways
如图所示，本发明包括原料气箱（1）、原料气增压泵（2）、吸收塔（3）、套管式微反应器（4）、活化剂哌嗪入口（5）、气液分离器（6）、液力透平（7）、循环泵（8）、闪蒸器（9）、贫富液换热器（10）、半贫液换热器（11）、再生塔（12）、再沸器（13）、冷却水箱（14）、热泵（15）、分离器（16）、酸水回流泵（17）、酸气回收箱（18）、半贫液后冷器（19）、贫液后冷器（20）、MDEA循环泵（21）、洗涤槽回流泵（22）、水洗涤槽（23）、处理气收集箱（24），套管式微反应器（4）设置在吸收塔（3）内一侧的腔体内，活化剂哌嗪入口（5）与套管式微反应器（4）外侧腔体连通设置在腔体下部，套管式微反应器（4）下端进口通过原料气增压泵（2）与原料气箱（1）相连。As shown in the figure, the present invention includes a feed gas tank (1), a feed gas booster pump (2), an absorption tower (3), a casing microreactor (4), an activator piperazine inlet (5), a gas-liquid Separator (6), hydraulic turbine (7), circulating pump (8), flash evaporator (9), lean-rich liquid heat exchanger (10), semi-lean liquid heat exchanger (11), regeneration tower (12 ), reboiler (13), cooling water tank (14), heat pump (15), separator (16), acid water reflux pump (17), acid gas recovery tank (18), semi-lean liquid aftercooler (19 ), lean liquid aftercooler (20), MDEA circulation pump (21), washing tank reflux pump (22), water washing tank (23), treated gas collection box (24), casing microreactor (4) In the cavity on one side of the absorption tower (3), the piperazine inlet (5) of the activator is connected to the outer cavity of the casing microreactor (4) and is arranged at the lower part of the cavity, and the inlet at the lower end of the casing microreactor (4) It is connected to the raw gas tank (1) through the raw gas booster pump (2).
套管式微反应器（4）上端出口上方的腔体上端设置有竖向出口，竖向出口与吸收塔（3）内上端的气液分离器（6）入口相连，气液分离器（6）上端气体出口与水洗涤槽（23）相连，水洗涤槽（23）的气体出口与处理气收集箱（24）相连，水洗涤槽（23）的液体出口通过洗涤槽回流泵（22）与竖向再生塔（12）的中部进口相连；气液分离器（6）远离腔体侧下端设置有向下的液体出口，液体出口与腔体外吸收塔（3）内空间连通，吸收塔（3）下端设置有与腔体外吸收塔（3）内空间连通的横向富液出口，富液出口与液力透平（7）的进口相连，液力透平（7）的出口通过闪蒸器（9）分别与贫富液换热器（10）、半贫液换热器（11）的第一换热通道入口相连，贫富液换热器（10）、半贫液换热器（11）的第一换热通道出口与再沸器（13）的富液进口相连。The upper end of the cavity above the upper outlet of the casing microreactor (4) is provided with a vertical outlet, and the vertical outlet is connected to the inlet of the gas-liquid separator (6) at the upper end of the absorption tower (3), and the gas-liquid separator (6) The upper gas outlet is connected to the water washing tank (23), the gas outlet of the water washing tank (23) is connected to the processing gas collection box (24), and the liquid outlet of the water washing tank (23) is connected to the vertical tank through the washing tank return pump (22). It is connected to the middle inlet of the regeneration tower (12); the gas-liquid separator (6) is provided with a downward liquid outlet at the lower end away from the chamber, and the liquid outlet communicates with the inner space of the absorption tower (3) outside the chamber, and the absorption tower (3) The lower end is provided with a horizontal rich liquid outlet connected to the inner space of the absorption tower (3) outside the cavity, the rich liquid outlet is connected to the inlet of the hydraulic turbine (7), and the outlet of the hydraulic turbine (7) passes through the flash evaporator (9) respectively connected to the inlet of the first heat exchange channel of the lean-rich liquid heat exchanger (10) and the semi-lean liquid heat exchanger (11); The outlet of the first heat exchange channel is connected with the rich liquid inlet of the reboiler (13).
液力透平（7）的驱动输出端与循环泵（8）的驱动输入端相连，循环泵（8）的出口同与套管式微反应器（4）外侧腔体连通设置在腔体下部的半贫液进口相连，循环泵（8）的进口通过半贫液后冷器（19）与半贫液换热器（11）的第二换热通道出口相连，半贫液换热器（11）的第二换热通道入口与再生塔（12）中部半贫液出口相连。The drive output end of the hydraulic turbine (7) is connected to the drive input end of the circulation pump (8), and the outlet of the circulation pump (8) communicates with the outer cavity of the casing microreactor (4) and is arranged at the lower part of the cavity. The inlet of the semi-lean liquid is connected, the inlet of the circulating pump (8) is connected with the outlet of the second heat exchange channel of the semi-lean liquid heat exchanger (11) through the semi-lean liquid aftercooler (19), and the semi-lean liquid heat exchanger (11 ) The inlet of the second heat exchange channel is connected with the semi-poor liquid outlet in the middle of the regeneration tower (12).
贫富液换热器（10）的第二换热通道入口与再生塔（12）下端贫液出口相连，贫富液换热器（10）的第二换热通道出口依次通过贫液后冷器（20）、MDEA循环泵（21）同与套管式微反应器（4）外侧腔体连通设置在腔体上部的贫液进口相连。The inlet of the second heat exchange channel of the lean-rich liquid heat exchanger (10) is connected to the lean liquid outlet at the lower end of the regeneration tower (12), and the outlet of the second heat exchange channel of the lean-rich liquid heat exchanger (10) passes through the lean liquid after-cooling successively. The device (20), MDEA circulation pump (21) is connected with the lean liquid inlet which is connected with the outer cavity of the casing microreactor (4) and arranged on the upper part of the cavity.
再沸器（13）的气体出口与再生塔（12）下部的气体入口相连，再沸器（13）的半贫液出口与再生塔（12）下部的液体入口相连；再生塔（12）下端的半贫液出口分别与再沸器（13）的半贫液入口、热泵（15）半贫液加热口相连。The gas outlet of the reboiler (13) is connected with the gas inlet of the lower part of the regeneration tower (12), and the semi-lean liquid outlet of the reboiler (13) is connected with the liquid inlet of the lower part of the regeneration tower (12); the lower end of the regeneration tower (12) The semi-lean liquid outlet of the reboiler (13) is connected with the semi-lean liquid inlet of the reboiler (13) and the semi-lean liquid heating port of the heat pump (15) respectively.
再沸器（13）的冷凝水出口与冷却水箱（14）的冷凝水入口相连，冷却水箱（14）的冷凝水出口与热泵（15）的换热液体进口相连，热泵（15）的换热液体出口与冷却水箱（14）的换热后冷凝水入口相连；热泵（15）的换热气体入口与再生塔（12）上端的热的酸水气出口相连，热泵（15）的换热后出口与分离器（16）的入口相连，分离器（16）的酸气出口与酸气回收箱（18）相连，分离器（16）的酸水出口通过酸水回流泵（17）与再生塔（12）上端的酸水回流口相连。The condensed water outlet of the reboiler (13) is connected with the condensed water inlet of the cooling water tank (14), the condensed water outlet of the cooling water tank (14) is connected with the heat exchange liquid inlet of the heat pump (15), and the heat exchange liquid of the heat pump (15) The liquid outlet is connected to the heat-exchanged condensed water inlet of the cooling water tank (14); the heat-exchanged gas inlet of the heat pump (15) is connected to the hot acid water gas outlet at the upper end of the regeneration tower (12); The outlet is connected to the inlet of the separator (16), the acid gas outlet of the separator (16) is connected to the acid gas recovery tank (18), the acid water outlet of the separator (16) is connected to the regeneration tower through the acid water reflux pump (17) (12) The acid water return port at the upper end is connected.
其中原料气箱（1）、酸气回收箱（18）、处理气收集箱（24）属于收集系统。原料气增压泵（2）、循环泵（8）、酸水回流泵（17）、MDEA循环泵（21）、洗涤槽回流泵（22）属于气液输送系统。套管式微反应器（4）、活化剂哌嗪入口（5）属于促进反应加快吸收系统。气液分离器（6）、分离器（16）属于气液分离系统。液力透平（7）、贫富液换热器（10）、半贫液换热器（11）、热泵（15）属于液体压力和气体热能回收系统。闪蒸器（9）、再沸器（13）属于降压与再沸辅助系统。Among them, the raw material gas box (1), the acid gas recovery box (18), and the treated gas collection box (24) belong to the collection system. Raw material gas booster pump (2), circulation pump (8), acid water return pump (17), MDEA circulation pump (21), and washing tank return pump (22) belong to the gas-liquid conveying system. The sleeve-type microreactor (4) and the piperazine inlet (5) of the activator belong to a reaction-promoting and absorption-accelerating system. The gas-liquid separator (6) and the separator (16) belong to the gas-liquid separation system. The hydraulic turbine (7), the lean-rich liquid heat exchanger (10), the semi-lean liquid heat exchanger (11), and the heat pump (15) belong to the liquid pressure and gas heat energy recovery system. The flash evaporator (9) and the reboiler (13) belong to the decompression and reboil auxiliary system.
所述半贫液后冷器（19）与半贫液换热器（11）的第二换热通道出口之间设置有阀门。A valve is provided between the semi-lean liquid aftercooler (19) and the outlet of the second heat exchange channel of the semi-lean liquid heat exchanger (11).
所述贫富液换热器（10）的第二换热通道入口与再生塔（12）下端贫液出口之间设置有阀门。A valve is provided between the inlet of the second heat exchange channel of the lean-rich liquid heat exchanger (10) and the lean liquid outlet at the lower end of the regeneration tower (12).
所述MDEA循环泵（21）与贫液进口之间设置有阀门。A valve is provided between the MDEA circulation pump (21) and the lean liquid inlet.
所述闪蒸器（9）顶端闪蒸气出口与再生塔（12）或酸气回收箱（18）相连。The flash gas outlet at the top of the flasher (9) is connected to the regeneration tower (12) or the acid gas recovery tank (18).
根据实际的填埋场运行状况建造满足规模的本工艺装置。在拼装时，可先做主要部分吸收塔（3）和再生塔（12）。在做吸收塔（3）时在其内部布置微型套管式反应器（4）和气液分离器（6）。接着根据工艺图纸布置液力透平（7）、闪蒸器（9）、贫富液换热器（10）、半贫液换热器（11）、再沸器（13）、贫液后冷气（20）、分离器（16）等主要部分。然后再安装一些循环泵和热泵。最后布置水洗涤槽（23）和气体装载装置。According to the actual operation status of the landfill site, the process device meeting the scale shall be constructed. When assembling, can do main part absorption tower (3) and regeneration tower (12) earlier. When the absorption tower (3) is made, a micro sleeve reactor (4) and a gas-liquid separator (6) are arranged inside it. Then arrange the hydraulic turbine (7), flash evaporator (9), lean-rich liquid heat exchanger (10), semi-lean liquid heat exchanger (11), reboiler (13), and lean liquid post-air conditioner according to the process drawings (20), separator (16) and other main parts. Then install some circulation pumps and heat pumps. Finally, the water washing tank (23) and the gas loading device are arranged.
所述再生塔可采用盛宝的sbhb型再生塔。The regeneration tower can be the sbhb regeneration tower of Saxo.
所述热泵可采用科莱泰克的CWW型热泵。The heat pump can adopt the CWW type heat pump of Kelaitech.
下面结合附图说明本发明的工作过程。The working process of the present invention will be described below in conjunction with the accompanying drawings.
液力透平（7）上方引线供给循环泵（8）能量由富液压力转换而来。闪蒸器（9）顶端出口线是闪蒸富液后，富液压力减小后所得的闪蒸气从富液中解析所得，闪蒸气体可以直接接入再生塔（12），也可以直接接入酸气回收箱（18）。经过换热器（10）、（11）后的富液直接从再沸器（13）下部进入，换热器（10）、（11）上方出口为半贫液，贫液换热出口。再沸器（13）左侧有两条进口进入再生塔（12），上进口线为一些在再沸器（13）升温后析出的气体，下进口线为半贫液加热回流进再生塔（12）。再沸器13右上进口为低压蒸汽用于再沸器（13）的工作，从再沸器（13）连入冷却水箱（14）为冷凝水，再沸器工作所得的产物。冷却水箱（14）左侧为冷凝水在热泵（15）中与热的酸气换热再经过热泵（15）吸收冷凝水中大部分热凝后回流进冷却水箱后（14）自然冷却。热泵（15）左下引线与要再沸的半贫液相连为热泵15吸收热能后给半贫液温度加热再进入再沸器（13）。热泵（15）左侧为酸气进口，上方为换热后出口。吸收塔（3）右侧上方进口为贫液进口，右侧下方为半贫液进口。刚从吸收塔（3）出来的气体经过水洗涤槽（23）洗涤后进入处理气收集箱（24）重新收集。水洗涤槽（23）中溶解剩余部分有害气体后，经过泵抽取回再生塔（12）处理。The lead wire above the hydraulic turbine (7) supplies the circulation pump (8) with energy converted from the pressure of the rich liquid. The outlet line at the top of the flash evaporator (9) is obtained by decomposing the flash gas obtained after the rich liquid is flashed and the pressure of the rich liquid is reduced. The flash gas can be directly connected to the regeneration tower (12) or directly connected to the Acid gas recovery tank (18). The rich liquid after passing through the heat exchangers (10) and (11) enters directly from the lower part of the reboiler (13), and the upper outlet of the heat exchangers (10) and (11) is semi-poor liquid, and the heat exchange outlet of the lean liquid. There are two inlets on the left side of the reboiler (13) to enter the regeneration tower (12), the upper inlet line is some gas that is precipitated after the reboiler (13) is heated up, and the lower inlet line is the semi-poor liquid that is heated and refluxed into the regeneration tower ( 12). The upper right inlet of reboiler 13 is low-pressure steam used for the work of reboiler (13), and is connected to cooling water tank (14) from reboiler (13) to be condensed water, the product of reboiler work gained. On the left side of the cooling water tank (14), the condensed water exchanges heat with the hot acid gas in the heat pump (15), and then passes through the heat pump (15) to absorb most of the condensation in the condensed water, and then flows back into the cooling water tank (14) for natural cooling. The heat pump (15) lower left lead is connected with the semi-lean liquid to be reboiled for the heat pump 15 to absorb heat energy and then enter the reboiler (13) to heat the semi-lean liquid temperature. The left side of the heat pump (15) is the acid gas inlet, and the top is the outlet after heat exchange. The upper right inlet of the absorption tower (3) is the lean liquid inlet, and the lower right side is the semi-poor liquid inlet. The gas just coming out of the absorption tower (3) is washed by the water washing tank (23) and then enters the treated gas collection box (24) for re-collection. After dissolving the remaining part of the harmful gas in the water washing tank (23), it is pumped back to the regeneration tower (12) for treatment.
可以理解的是，以上关于本发明的具体描述，仅用于说明本发明而并非受限于本发明实施例所描述的技术方案，本领域的普通技术人员应当理解，仍然可以对本发明进行修改或等同替换，以达到相同的技术效果；只要满足使用需要，都在本发明的保护范围之内。It can be understood that the above specific descriptions of the present invention are only used to illustrate the present invention and are not limited to the technical solutions described in the embodiments of the present invention. Those of ordinary skill in the art should understand that the present invention can still be modified or Equivalent replacements to achieve the same technical effect; as long as they meet the needs of use, they are all within the protection scope of the present invention.
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|---|---|---|---|---|
| US4775519A (en) * | 1985-10-31 | 1988-10-04 | Texaco Inc. | Removal of acid gases from gas streams |
| EP2125164A1 (en) * | 2007-01-25 | 2009-12-02 | Shell Internationale Research Maatschappij B.V. | Process for producing a pressurised co2 stream in a power plant integrated with a co2 capture unit |
| CN102657998A (en) * | 2012-04-25 | 2012-09-12 | 中国石油化工股份有限公司 | Mixed solvent for removing acid gas |
| CN205850531U (en) * | 2016-07-20 | 2017-01-04 | 辽宁工业大学 | A kind of double-tower type MEDA processes landfill gas system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4775519A (en) * | 1985-10-31 | 1988-10-04 | Texaco Inc. | Removal of acid gases from gas streams |
| EP2125164A1 (en) * | 2007-01-25 | 2009-12-02 | Shell Internationale Research Maatschappij B.V. | Process for producing a pressurised co2 stream in a power plant integrated with a co2 capture unit |
| CN102657998A (en) * | 2012-04-25 | 2012-09-12 | 中国石油化工股份有限公司 | Mixed solvent for removing acid gas |
| CN205850531U (en) * | 2016-07-20 | 2017-01-04 | 辽宁工业大学 | A kind of double-tower type MEDA processes landfill gas system |
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