CN220424983U - Wet flue gas decarbonization equipment - Google Patents
Wet flue gas decarbonization equipment Download PDFInfo
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- CN220424983U CN220424983U CN202321470346.9U CN202321470346U CN220424983U CN 220424983 U CN220424983 U CN 220424983U CN 202321470346 U CN202321470346 U CN 202321470346U CN 220424983 U CN220424983 U CN 220424983U
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- 239000003546 flue gas Substances 0.000 title claims abstract description 111
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 238000005262 decarbonization Methods 0.000 title claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 65
- 238000003795 desorption Methods 0.000 claims abstract description 48
- 238000010521 absorption reaction Methods 0.000 claims abstract description 42
- 238000005406 washing Methods 0.000 claims abstract description 30
- 239000002904 solvent Substances 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 239000012535 impurity Substances 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 25
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- 238000002360 preparation method Methods 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 18
- 229910052799 carbon Inorganic materials 0.000 description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 16
- 239000000243 solution Substances 0.000 description 15
- 238000005261 decarburization Methods 0.000 description 11
- 239000000047 product Substances 0.000 description 10
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 description 8
- 238000001816 cooling Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 238000004891 communication Methods 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 230000009919 sequestration Effects 0.000 description 2
- 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 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- 241000220225 Malus Species 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- -1 alcohol amine Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 229940072033 potash Drugs 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present utility model relates to CO 2 The technical field of preparation discloses a wet flue gas decarbonization's equipment, include: the device comprises a water washing unit, an absorption unit, a desorption unit and a thermal cycle unit; the water washing unit is connected with the flue gas feeding pipe 11 and is used for washing hot flue gas to remove water-soluble impurities; the absorption unit is connected with the water washing unit and is used for contacting the flue gas after water washing with the solvent to enable the solvent to absorb CO in the flue gas 2 Forming a richA liquid; the desorption unit is connected with the absorption unit and comprises a stripping part for stripping and desorbing the rich liquid to obtain CO 2 And a lean solution; and the thermal circulation unit is used for collecting the flue gas heat of the hot flue gas in the flue gas feeding pipe and the heat of the discharged material of the desorption unit, and providing the two heat to the stripping part. The utility model has the advantages of saving energy consumption and reducing CO 2 The manufacturing cost of the product is improved.
Description
Technical Field
The present utility model relates to CO 2 The technical field of the preparation and the preparation,in particular to wet flue gas decarburization equipment.
Background
The carbon emission source of China is combined, and the carbon neutralization of the whole society is realized by the following aspects:
realizes energy structure conversion, and replaces fossil fuel by clean energy such as nuclear energy. China may need to adjust the primary energy structure from 85% of current fossil fuels to 85% of clean energy. Searching a new hydrogen production path, and realizing decarburization of the hydrogen production process by combining the use of clean energy. Carbon sinks and carbon capture, utilization and sequestration technologies have been developed. At present, the carbon quota of China is a mechanism for free allocation and spot transaction, and under the background of carbon neutralization, the energy consumption of ten thousand-yuan GDP in China is reduced by 13.5% in the period from 2021 to 2025, so that the future carbon quota is further contracted. As the carbon emission market matures, the price of carbon trade will reach 300-500 yuan/ton CO 2 . For high energy consumption enterprises, the excess of carbon emission leads to a significant increase in production cost, so that new technology can be developed only by eliminating the original old energy consumption technology or additional CO can be added beyond carbon by a carbon capture technology 2 And collecting the waste water.
In the next 20 years, the energy structure of China is expected not to be changed greatly, so that the large-scale carbon capture, utilization and sequestration (CCUS) is the only solution which can be applied to the existing most difficult major industrial facilities for emission reduction in the next 20-30 years at present and realizes remarkable and direct emission reduction.
In CO 2 Utilization of CO 2 The main modes available are enhanced oil recovery, facility agriculture, chemical conversion, food processing and the like. According to investigation, CO capable of being used for enhancing oil displacement 2 The amount is expected to exceed 4000 ten thousand tons/year, CO 2 Annual oil production can reach tens of millions of tons scale, CO 2 The potential for EOR is enormous. The facility agriculture develops the carbon sink effect of crops by additionally applying carbon dioxide gas fertilizer. The carbon absorption rate of the crop is about 0.007 t/(m) -2 ·a -1 ) If the facility agriculture is utilized to realize annual trapping of 10 ten thousand tCO 2 The required crop area is about 30km 2 I.e. 4-5 ten thousand acres. In 2012, the agricultural area of the facility in China is 5796 ten thousand muAccounting for more than 85 percent of the total world area, and the maximum available CO 2 Reaching one hundred million tons per year. However, due to the wide distribution of facility agriculture, the area of crops required for a conventional-scale carbon capture project is large, and it is difficult to realize larger-scale CO 2 Utilization. Chemical conversion of present Total CO 2 The utilization was about 25 ten thousand tons and still in pilot plant phase. CO for food processing 2 There are few.
In summary, EOR is the only way to achieve large scale CO2 utilization. The combination of CCS and EOR allows for large-scale carbon capture and utilization. However, the current carbon capture cost is too high, and the method is still a key for influencing the large-scale popularization of the CCS-EOR technology.
Disclosure of Invention
The utility model aims to overcome the defects of CO existing in the prior art 2 The problem of overall high energy consumption and cost of the trapping technology is solved, and the wet flue gas decarburization equipment is provided, which has the advantages of saving energy consumption and reducing CO 2 The manufacturing cost of the product is improved.
In order to achieve the above object, the present utility model provides an apparatus for decarbonizing wet flue gas, the apparatus for decarbonizing wet flue gas comprising:
the water washing unit is connected with the flue gas feeding pipe and is used for washing hot flue gas to remove water-soluble impurities;
the absorption unit is connected with the water washing unit and is used for contacting the flue gas subjected to water washing with a solvent to enable the solvent to absorb CO in the flue gas 2 Forming a rich solution;
the desorption unit is connected with the absorption unit and comprises a stripping part for stripping and desorbing the rich liquid to obtain CO 2 And a lean solution;
and the thermal circulation unit is used for collecting the flue gas heat of the hot flue gas in the flue gas feeding pipe and providing the flue gas heat to the stripping part.
In some embodiments of the utility model, the thermal cycle unit comprises a first heat exchange portion and a second heat exchange portion in communication, wherein the first heat exchange portion is used for collecting flue gas heat of the hot flue gas in the flue gas feed pipe, and the second heat exchange portion is used for providing the flue gas heat collected by the first heat exchange portion to the stripping portion.
In some embodiments of the utility model, the thermal cycle unit further comprises a third heat exchange section for collecting CO desorbed from the desorption unit 2 CO of (c) 2 The third heat exchange part is communicated with the second heat exchange part and is used for converting the CO 2 Heat and heat of the solution vapor are provided to the stripping section.
Through the technical scheme, the wet flue gas decarburization equipment aims at integrating the cooling and heating requirements in the wet decarburization process, and takes the heat of the hot flue gas as the heat source of the stripping part, and further takes the heat of the hot flue gas and the heat of the discharged materials of the desorption tower as the heat sources, so that the energy consumption is saved, and the CO is reduced 2 Is a cost of manufacture.
Drawings
FIG. 1 is a schematic diagram of the wet flue gas decarbonization apparatus according to an embodiment of the present utility model;
FIG. 2 is a flow chart of comparative example 1 of the present utility model.
Description of the reference numerals
1, a water washing tower; 11 smoke feeding pipe; 12 a wash water feed line; 2 an absorption tower; 21 a solvent feed line; 3, a desorption tower; 31 a desorption part; 32 stripping section; 33CO 2 A product gas discharging pipe; 4, a production pipe; 5 a first heat exchanger; 6 a third heat exchanger; 7, reboiler; 8, separating a tank; 9 heat pump compressor.
Detailed Description
In the present utility model, unless otherwise specified, terms such as "upper, lower, left, and right" and "upper, lower, left, and right" are used generically to refer to the upper, lower, left, and right illustrated in the drawings; "inner and outer" means the inner and outer relative to the outline of each component itself, and "top" of the vessel means the position of the vessel from top to bottom by 0-30% unless specified; the "upper portion" of the container refers to the position of the container from top to bottom by 0-50%; the "lower portion" of the vessel refers to the position of the vessel from bottom to top of 0-50%, and the "bottom" of the vessel refers to the position of the vessel from bottom to top of 0-30%.
In CCS technology, post-combustion flue gas absorption is still the most dominant and simple way. Among them, the chemical absorption method is dominant. The chemical absorption method mainly comprises a hot potassium alkali method, an ammonia method, an alcohol amine method and the like, and the advantages and disadvantages and industrial application examples thereof are shown in the following table 1.
Table 1: comparison and Industrial examples of several decarbonization methods
| Method | Advantages are that | Disadvantages | Industrial application example |
| Hot potash | The solution has strong CO2 absorption capacity and loss of organic components Low purity of regenerated gas, high and low cost | High regeneration energy consumption | Malus natural gasification factory and peak-building chemical fertilizer Chemical fertilizer plant for petrochemical sauvignon of Jinling |
| Ammonia process | Low cost, and the CO2 removal efficiency reaches 95 to 99 percent About, by-product bicarbonate, low desorption energy consumption | Ammonia water cyclic utilization rate caused by ammonia escape Low and difficult separation of NH3 and CO2 | Guangxi water conservancy electric power construction group limited public Tian Dong power plant |
| MEA method | Low cost, CO2 absorptionThe rate of recovery is fast, and the energy is absorbed Strong force | High regeneration energy consumption | Most of thermal power plants |
| MDEA process | High absorption capacity and low energy consumption | Low rate of CO2 absorption | Wulu in eastern natural gas treatment plant of Zhonghai oil Chemical fertilizer plant of wood-alignment petrochemical company |
CO 2 Overall cost of capture technology is high, wherein CO 2 The cost of capture separation is about 70-80% of the total cost of CCS, thus reducing CO 2 The cost of the capture separation is of great importance. Based on analysis of the cost of the absorption process, CO 2 The high desorption energy consumption is a main reason for the high cost of the absorption method. The water evaporation latent heat and the absorbent heating sensible heat in the desorption energy consumption account for 40-50% of the total desorption energy consumption, so that the CO separation with low cost and high efficiency is realized 2 There is a need to develop a low energy consumption flue gas decarbonization process.
In order to solve the problems, the utility model discloses wet flue gas decarburization equipment, which comprises:
the water washing unit is connected with the flue gas feeding pipe 11 and is used for washing hot flue gas to remove water-soluble impurities;
the absorption unit is connected with the water washing unit and is used for contacting the flue gas after water washing with the solvent to enable the solvent to absorb CO in the flue gas 2 Forming a rich solution;
a desorption unit connected with the absorption unit and comprising a stripping part 32 for stripping and desorbing the rich liquid to obtain CO 2 And a lean solution;
and a thermal circulation unit for collecting the heat of the hot flue gas in the flue gas feed pipe and supplying the heat of the flue gas to the stripping section 32.
The wet flue gas decarburization equipment of the utility model aims at integrating the cooling and heating requirements in the wet decarburization process and takes the heat of the hot flue gas as the heat source of the stripping part 32, thereby saving energy consumption and reducing CO 2 Is a cost of manufacture.
To further save energy consumption and costs, in some embodiments of the utility model, the thermal cycle unit comprises a first heat exchange portion and a second heat exchange portion in communication, wherein the first heat exchange portion is configured to collect flue gas heat from the hot flue gas in the flue gas feed pipe, and the second heat exchange portion is configured to provide the flue gas heat collected by the first heat exchange portion to the stripping portion 32.
To further save energy and costs, in some embodiments of the utility model, the thermal cycle unit further comprises a third heat exchange section for collecting CO desorbed from the desorption unit 2 CO of (c) 2 The third heat exchange part is communicated with the second heat exchange part and is used for converting the CO 2 Heat is provided to the stripping section 32.
In some embodiments of the utility model, as shown in fig. 1, the water wash unit comprises a water wash column 1, the water wash column 1 being connected with a flue gas feed pipe 11 and a wash water feed pipe 12; further, the flue gas feed pipe 11 is connected to the lower part of the water scrubber 1, and the discharge port of the wash water feed pipe 12 is connected to the upper part of the water scrubber 1, so that the wash water fed through the wash water feed pipe 12 can be in countercurrent contact with the hot flue gas fed through the flue gas feed pipe 11.
In order to further save energy consumption and cost, in some embodiments of the present utility model, it is more preferable that the wash water feed pipe 12 is connected to the bottom of the water scrubber 1 and provided with a delivery pump, so as to implement the circulation of the wash water falling to the bottom of the water scrubber 1 back to the upper portion of the water scrubber 1.
In some embodiments of the utility model, the absorption unit comprises an absorption column 2, the absorption column 2 being in communication with the water wash column 1 and in communication with a solvent feed line 21, the solvent feed line 21For introducing a solvent for absorbing carbon dioxide into the absorption tower 2 and enabling the solvent to be in countercurrent contact with the flue gas after water washing to obtain the CO absorption 2 Is rich in (2); in the utility model, in order to realize countercurrent contact of the solvent and the washed flue gas, the lower part of the absorption tower 2 is communicated with the top of the water washing tower 1, the flue gas is introduced into the absorption tower 2, the solvent feeding pipe 21 is communicated with the upper part of the water washing tower 2, the solvent contacts with the flue gas from top to bottom, and the solvent contacts CO in the flue gas 2 The flue gas which cannot be absorbed is absorbed and becomes tail gas, and the tail gas is discharged from a tail gas outlet formed in the top of the absorption tower 2, so that the utility model has no special requirement on the absorption tower, for example, the tail gas outlet at the top can be connected with a tail gas treatment device in the prior art, the tail gas treatment accords with the discharge standard and is discharged into the atmosphere, for example, a sprayer for dispersing a solvent and the like can be arranged in the absorption tower, and the details are omitted.
In some embodiments of the present utility model, the desorption unit includes a desorption column 3, as shown in fig. 1, the desorption column 3 may be a conventional desorption column (or regeneration column) including a desorption portion 31 and a stripping portion 32 which are connected, the desorption portion 31 being connected to the absorption column 2, the stripping portion 32 being for providing steam to the desorption portion 31 and allowing the rich liquid from the absorption column 2 to be in countercurrent contact with steam (e.g., water vapor), and performing desorption to obtain lean liquid and CO 2 The method comprises the steps of carrying out a first treatment on the surface of the In the utility model, in order to realize countercurrent contact of vapor and rich liquid, a stripping part 32 is positioned at the lower part of a stripping tower 3, a stripping part 31 is positioned above the stripping part 32, the top part of the stripping part is communicated with the bottom of an absorption tower 2 so as to enable the rich liquid to enter from top to bottom in the tower, the stripping part 31 is communicated with the stripping part 32 and is also provided with a recovery pipe 4 to form an external circulation, and the recovery pipe 4 is provided with a reboiler 7 which can further desorb CO 2 The reboiler of the utility model can be a conventional reboiler, and the utility model has no special requirement for the reboiler and is not repeated.
To return lean liquid regenerated from rich liquid to the absorption tower 2 to absorb CO 2 In the present utility model, the stripping part 32 is connected to the solvent feed pipe 21 via a pipe, and for further energy saving, a lean-rich liquid heat exchanger may be provided on the pipe to preheat the lean liquid drawn from the desorption tower, for preheating the lean liquid fed from the absorption tower to the desorption towerThe lean solution after heat exchange can be cooled and then enters the absorption tower.
Further, to desorb CO 2 And part of solution steam is discharged, and the desorption tower 3 is connected with CO 2 A product gas discharge pipe 33; in the present utility model, there is no special requirement for the desorber, for example, CO 2 The product gas discharging pipe 33 is communicated with a water cooler, the water cooler is communicated with a underground tank which is communicated with the desorption tower 3, and a product gas outlet is formed in the water cooler, and the water cooler is used for discharging CO from the desorption tower 3 2 Condensing, condensing CO 2 The condensed water is discharged from the product gas outlet, and the separated condensed water enters the underground tank and returns to the desorption tower 3, and is not described herein.
In some embodiments of the utility model, to collect the flue gas heat of the hot flue gas in the flue gas feed, as shown in fig. 1, the first heat exchange section comprises a first heat exchanger 5 mounted on a flue gas feed 11; for collecting CO desorbed from the desorption unit 2 CO of (c) 2 The third heat exchange part comprises CO arranged between the water cooler and the desorption tower 3 2 A third heat exchanger 6 on the product gas discharge pipe 33; to provide the stripping section 32 with the collected flue gas heat and the overhead vapor heat of the desorber 3, the second heat exchange section comprises a reboiler 7 mounted on the extraction pipe 4.
In order to realize the heat collection and output utilization, so as to save energy consumption and cost, in some embodiments of the utility model, a flue gas feeding pipe 11 is communicated with a shell side of a first heat exchanger 5, and a tube side of the first heat exchanger 5 forms a first circulating pipe for circulating a heat exchange working medium (the utility model has no special requirement on the heat exchange working medium, and the conventional heat exchange working medium capable of meeting the heat exchange function in the prior art) and is communicated with a separation tank 8 and a collection tank; CO 2 The product gas discharging pipe 33 is communicated with the shell side of the third heat exchanger 6, the tube side of the third heat exchanger 6 forms a third circulating pipe for circulating heat exchange working media, and a separating tank 8 and a collecting tank are connected in the third circulating pipe; the shell side of the reboiler 7 communicates with the separation tank 8 and the collection tank through a second circulation pipe, and the production pipe 4 is formed as the tube side of the reboiler 7.
To further save energy consumption and cost, in the utility modelIn some embodiments of (2) a heat pump compressor 9 is arranged on the second circulation pipe, so that the heat of the hot flue gas and the heat of the discharge material of the desorber (comprising CO 2 CO discharged from the product gas discharge pipe 33 2 Heat and heat of solution vapor) is subjected to temperature and pressure raising by the heat pump compressor 9 and then enters the stripping part 32, and the heat pump compressor 9 can be selected from one of a centrifugal compressor, a screw compressor and a reciprocating compressor, and has no special requirements on the type of working medium of the heat pump compressor, including but not limited to fluorocarbon refrigerants (such as R245, R600a or R123), alcohol refrigerants, water or composite working medium.
In the prior art, a process for cooling hot flue gases and desorber overhead (comprising mainly desorbed CO 2 And carry vapor) consume a large amount of cooling water, and the process has larger energy waste, and according to the disclosure of the utility model, the utility model aims to integrate the cooling and heating requirements in the current wet decarburization process, and uses the heat pump technology to take the heat of flue gas and the vapor at the top of the desorption tower as the heat source of the desorption tower, thereby saving the consumption of vapor and cooling water and reducing CO 2 For the purpose of cost of manufacture.
In the utility model, various pipelines, control valves, pumps, separating tanks, collecting tanks or meters and other conventional parts which may be used in industry can be added to each part according to the needs, and the utility model has no special requirements.
The utility model also discloses a wet flue gas decarburization method, which comprises the following steps:
1) Washing the hot flue gas with water to remove water-soluble impurities;
2) Contacting the water-washed flue gas with a solvent to obtain the CO-absorbed flue gas 2 Is rich in (2);
3) Stripping and desorbing the rich liquid to obtain CO 2 And a lean solution;
wherein, the flue gas heat of the hot flue gas before the water washing in the step 1) is collected, and the flue gas heat is used for stripping and desorption in the step 3).
The utility model integrates the cooling and heating requirements in the wet decarburization processThe heat of the hot flue gas is used as a heat source, thereby saving energy consumption and reducing CO 2 Is a cost of manufacture.
To further save energy consumption and costs, the method of the utility model further comprises: the heat of the discharged material in the step 3) is collected for stripping desorption in the step 3).
In some embodiments of the utility model, the hot flue gas is from at least one of a coal boiler tail gas, a natural gas boiler tail gas, or an oil boiler tail gas.
In some embodiments of the utility model, the temperature of the hot flue gas is 80-250 ℃.
In some embodiments of the utility model, the flue gas temperature after the water wash in step 2) is less than or equal to 50 ℃.
In some embodiments of the utility model, the water-soluble impurities include SO 2 、NO x At least one of dust and oil.
In some embodiments of the utility model, the solvent comprises at least one of an aqueous monoethanolamine solution, an aqueous diethanolamine solution, or an aqueous methyldiethanolamine solution.
In some embodiments of the utility model, the contacting conditions in step 2) include a temperature in the range of 40-50 ℃ and atmospheric pressure.
In some embodiments of the utility model, the conditions of stripping desorption in step 3) include: the temperature is 100-130 deg.C and the pressure is 0.1-0.2Mpa.
In some embodiments of the utility model, the lean liquid in step 3) is returned to step 2) for contact with the water-washed flue gas to absorb CO 2 。
The present utility model will be described in detail by way of examples, but the present utility model is not limited thereto.
Example 1
The apparatus for decarbonizing wet flue gas shown in FIG. 1 was used to treat about 40,000Nm of a certain plant 3 The flow of the hot flue gas after desulfurization and denitrification by the coal boiler at/h comprises the following steps:
the temperature of the hot flue gas is 150-180 ℃, the heat of the recovered flue gas enters the low-pressure liquid methanol through the first heat exchanger 5, and then the flue gas passes throughPassing through a water scrubber 1, contacting with washing water, cooling to 40deg.C, and feeding into an absorber 2 by a blower, wherein CO 2 Is absorbed by monoethanolamine aqueous solution (mass concentration is 20%), tail gas is discharged into atmosphere from a tail gas outlet at the top of the tower, and CO is absorbed 2 The rich liquid after the heat recovery is sent to the desorption tower 3 through the lean-rich liquid heat exchanger from the tower bottom. De-aspirating CO 2 Cooling with water vapor by a third heat exchanger 6, recovering part of heat to give low pressure liquid methanol, separating to remove water to obtain CO 2 The product gas with the purity of 99 percent is sent to the subsequent working section for use.
The low-pressure liquid methanol of the heat exchange working medium circularly flows among the first heat exchanger 5, the third heat exchanger 6, the reboiler 7 and the centrifugal compressor 9, wherein heat is recovered in the first heat exchanger 5 and the third heat exchanger 6, the heat is evaporated into gas phase, the gas phase enters the centrifugal compressor, the pressure and the temperature rise, the gas phase is taken as a heat source and enters the reboiler 7 of the desorption tower 3, the heat is output, the cooled and liquefied heat exchange working medium enters the collecting tank, and the liquid phase of the collecting tank is continuously circulated.
Example 1 energy consumption the following table 1:
TABLE 1
Comparative example 1
Unlike example 1, the heat cycle unit, i.e., the first heat exchanger 5, the third heat exchanger 6 and the heat pump compressor 9 were not provided, and heat was not recovered for the reboiler 7, as shown in fig. 2, and the energy consumption of comparative example 1 is as follows in table 2:
TABLE 2
In contrast, the improved process flow, unit CO 2 The comprehensive energy consumption and the production cost are reduced compared with the traditional process.
The preferred embodiments of the present utility model have been described in detail above, but the present utility model is not limited thereto. Within the scope of the technical idea of the utility model, a number of simple variants of the technical solution of the utility model are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the utility model, all falling within the scope of protection of the utility model.
Claims (10)
1. An apparatus for decarbonizing wet flue gas, characterized in that the apparatus for decarbonizing wet flue gas comprises:
the water washing unit is connected with the flue gas feeding pipe (11) and is used for washing hot flue gas to remove water-soluble impurities;
the absorption unit is connected with the water washing unit and is used for contacting the flue gas subjected to water washing with a solvent to enable the solvent to absorb CO in the flue gas 2 Forming a rich solution;
a desorption unit connected with the absorption unit and comprising a stripping part (32) for stripping and desorbing the rich liquid to obtain CO 2 And a lean solution;
and the thermal circulation unit is used for collecting the flue gas heat of the hot flue gas in the flue gas feeding pipe and providing the flue gas heat to the stripping part (32).
2. The wet flue gas decarbonizing apparatus according to claim 1, wherein the thermal cycle unit comprises a first heat exchange portion and a second heat exchange portion which are communicated, wherein the first heat exchange portion is used for collecting flue gas heat of the hot flue gas in the flue gas feed pipe, and the second heat exchange portion is used for providing the flue gas heat collected by the first heat exchange portion to the stripping portion (32);
the thermal cycle unit also comprises a third heat exchange part, wherein the third heat exchange part is used for collecting heat of discharged materials in the desorption unit, and the third heat exchange part is communicated with the second heat exchange part and is used for providing the heat of the discharged materials to the stripping part (32).
3. Wet flue gas decarbonizing apparatus according to claim 1, characterized in that the water washing unit comprises a water washing tower (1), the water washing tower (1) is connected with the flue gas feed pipe (11) and a washing water feed pipe (12), and the washing water fed by the washing water feed pipe (12) is in countercurrent contact with the hot flue gas fed by the flue gas feed pipe (11).
4. A wet flue gas decarbonizing apparatus according to claim 3, characterized in that the wash water feed pipe (12) communicates with the bottom of the water scrubber (1) for circulating the wash water falling to the bottom of the water scrubber (1) back to the upper part of the water scrubber (1).
5. The wet flue gas decarbonization apparatus according to claim 3 or 4, wherein the absorption unit comprises an absorption tower (2), the absorption tower (2) is connected to the water scrubber (1) and to a solvent feed pipe (21), the solvent feed pipe (21) is used for introducing solvent into the absorption tower (2), and the solvent is in countercurrent contact with the water scrubbed flue gas to obtain CO-absorbed 2 Is rich in (a) a liquid rich in (b).
6. The wet flue gas decarbonizing apparatus according to claim 4, wherein the desorption unit comprises a desorption tower (3), the desorption tower (3) comprises a desorption part (31) and a stripping part (32) which are communicated, the desorption part (31) is communicated with the absorption tower (2), the stripping part (32) is used for providing steam for the desorption part (31) and allowing the rich liquid from the absorption tower (2) to be in countercurrent contact with the steam for desorption to obtain lean liquid and CO 2 ；
The desorption tower (3) is connected with CO 2 A product gas outlet (33) for desorbing CO 2 And part of the solution vapor is discharged.
7. The wet flue gas decarbonization apparatus according to claim 6, wherein the stripping section (32) is located at the lower part of the stripping tower (3), the stripping section (31) is located above the stripping section (32), the stripping section (31) is communicated with the stripping section (32) through a extraction pipe (4), and a reboiler (7) is installed on the extraction pipe (4); and/or
The stripping part (32) is communicated with a solvent feeding pipe (21) for returning the lean liquid to the absorption tower (2) for absorbing CO 2 。
8. Wet flue gas decarbonizing apparatus according to claim 2, characterized in that the first heat exchange section comprises a first heat exchanger (5) mounted on a flue gas feed pipe (11), the second heat exchange section comprises a reboiler (7), and the third heat exchange section comprises CO mounted between a water cooler and a desorption tower (3) 2 And a third heat exchanger (6) on the product gas discharging pipe (33).
9. The wet flue gas decarbonizing device according to claim 8, wherein the flue gas feeding pipe (11) is communicated with a shell side of the first heat exchanger (5), a first circulating pipe for circulating heat exchange working media is formed on the tube side of the first heat exchanger (5), and a separation tank (8) is communicated in the first circulating pipe;
the CO 2 The product gas discharging pipe (33) is communicated with the shell side of the third heat exchanger (6), the tube side of the third heat exchanger (6) forms a third circulating pipe for circulating heat exchange working media, and the separating tank (8) is connected in the third circulating pipe;
the shell side of the reboiler (7) is communicated with the separation tank (8) through a second circulating pipe, and the extraction pipe (4) is formed into the tube side of the reboiler (7).
10. The wet flue gas decarbonizing apparatus according to claim 9, wherein a heat pump compressor (9) is provided on the second circulation pipe, wherein the heat pump compressor (9) is selected from one of a centrifugal compressor, a screw compressor or a reciprocating compressor.
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| CN202321470346.9U CN220424983U (en) | 2023-06-09 | 2023-06-09 | Wet flue gas decarbonization equipment |
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| CN202321470346.9U CN220424983U (en) | 2023-06-09 | 2023-06-09 | Wet flue gas decarbonization equipment |
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