CN114939331A - Sulfur-carbon synergetic integrated wet-process removal device - Google Patents
Sulfur-carbon synergetic integrated wet-process removal device Download PDFInfo
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- CN114939331A CN114939331A CN202210649906.0A CN202210649906A CN114939331A CN 114939331 A CN114939331 A CN 114939331A CN 202210649906 A CN202210649906 A CN 202210649906A CN 114939331 A CN114939331 A CN 114939331A
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- GJEAMHAFPYZYDE-UHFFFAOYSA-N [C].[S] Chemical compound [C].[S] GJEAMHAFPYZYDE-UHFFFAOYSA-N 0.000 title claims description 16
- 238000000034 method Methods 0.000 title claims description 7
- 230000002195 synergetic effect Effects 0.000 title description 8
- 238000010521 absorption reaction Methods 0.000 claims abstract description 113
- 239000007788 liquid Substances 0.000 claims abstract description 70
- 238000005507 spraying Methods 0.000 claims abstract description 34
- 230000002745 absorbent Effects 0.000 claims abstract description 33
- 239000002250 absorbent Substances 0.000 claims abstract description 33
- 230000008929 regeneration Effects 0.000 claims abstract description 30
- 238000011069 regeneration method Methods 0.000 claims abstract description 30
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 26
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 26
- 239000011593 sulfur Substances 0.000 claims abstract description 26
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000007921 spray Substances 0.000 claims abstract description 12
- 238000003795 desorption Methods 0.000 claims abstract description 11
- 239000012535 impurity Substances 0.000 claims description 22
- 239000003513 alkali Substances 0.000 claims description 20
- 238000012856 packing Methods 0.000 claims description 16
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- 239000000243 solution Substances 0.000 description 9
- 238000000746 purification Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 125000005842 heteroatom Chemical group 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000004065 semiconductor Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000005067 remediation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Biomedical Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a sulfur and carbon cooperative integrated wet removal device, which comprises a pretreatment bell mouth, a sulfur and carbon integrated removal tower, absorbent regeneration and CO 2 Desorption system, absorbent regeneration and SO 2 The pretreatment bell mouth is connected with an inlet of the sulfur and carbon integrated removing tower, and SO is sequentially arranged on the sulfur and carbon integrated removing tower from bottom to top 2 Absorption zone, CO 2 An absorption zone, a demisting system, the SO 2 Absorption zone, CO 2 The absorption zone is provided with a plurality of first and second spray layers, and the bottom is provided with a first and second absorption liquid collecting systemA system; the output end of the first absorption liquid collecting system is respectively connected with the absorbent regeneration and SO after being shunted by the first PH sorting system 2 The system comprises an analysis system and a first spraying layer; the output end of the second absorption liquid collecting system is respectively connected with the absorbent regeneration and the CO after being shunted by the second PH sorting system 2 Analytic system, second spray layer. The device can economically and efficiently realize the integrated removal of sulfur and carbon, and has small occupied area and low cost.
Description
[ technical field ] A method for producing a semiconductor device
The invention relates to the technical field of pollutant treatment, in particular to a sulfur-carbon synergistic integrated wet removal device.
[ background ] A method for producing a semiconductor device
With the rapid development of economy and society in China, the problems of energy and environment are increasingly highlighted. The energy pattern mainly based on coal in China does not change greatly in a long period of time, and the flue gas generated by a coal-fired power plant contains various gaseous or solid pollutants such as SO 2 、NO x And particulate matter PM10 or PM2.5, etc. having a particle diameter of less than 20 μm or 2.5 μm, although CO 2 Has not been included as an object for the remediation of atmospheric pollutants, but is gaining increasing attention due to its greenhouse effect, with power plants being the largest CO 2 One of the fixed emission sources. The existing cooperative removal equipment mostly adopts the modes of wet desulphurization, pretreatment and carbon capture, has complex process, high cost and large occupied area, and provides a sulfur-carbon cooperative integrated wet removal device.
[ summary of the invention ]
The invention aims to solve the problems in the prior art and provides a sulfur and carbon synergistic integrated wet removal device which can economically and efficiently realize the integrated removal of sulfur and carbon, and has the advantages of small occupied area and low cost.
In order to realize the purpose, the invention provides a sulfur and carbon synergistic integrated wet removal device, which comprises a pretreatment bell mouth, a sulfur and carbon integrated removal tower, absorbent regeneration and CO 2 Desorption system, absorbent regeneration and SO 2 The output end of the pretreatment bell mouth is connected with an inlet of the sulfur and carbon integrated removing tower, and the sulfur and carbon integrated removing tower is sequentially provided with SO from bottom to top 2 Absorption zone, CO 2 An absorption zone, a demisting system, the SO 2 Absorption zone, said CO 2 A plurality of first spraying layers and second spraying layers are respectively arranged in the absorption area, and the SO 2 Absorption zone, CO 2 The bottom of the absorption area is respectively provided with a first absorption liquid collecting system and a second absorption liquid collecting system, and the second absorption liquid collecting system is provided with an auxiliary channel through which air flow can pass; the output end of the first absorption liquid collecting system is respectively connected with the absorbent regeneration and SO after being shunted by the first PH sorting system 2 The analysis system and the first spraying layer; the output end of the second absorption liquid collecting system is respectively connected with the absorbent regeneration and the CO after being shunted by the second PH sorting system 2 Analytic system, second spray layer.
Preferably, an output end of the first PH sorting system is connected with the first impurity removing system and then connected to the first spraying layer, and the first PH sorting system is used for collecting SO output by the first absorption liquid collecting system 2 Shunting the absorption liquid according to the pH value; when the SO is input into the first PH sorting system 2 SO when the pH of the absorption solution is above 4.5 2 The absorption liquid is conveyed to a first spraying layer after impurities are removed by an impurity removing system; when SO is input into the first PH sorting system 2 When the pH value of the absorption liquid is less than 4.5, the absorption liquid is conveyed to the absorbent for regeneration and SO 2 And (5) analyzing the system.
Preferably, one output end of the second PH sorting system is connected with the second impurity removal system and then connected to the second spraying layer, and the second PH sorting system is used for collecting CO output by the second absorption liquid collection system 2 Absorption liquid according to pH valueA stream; when CO is input into the second PH sorting system 2 When the pH of the absorption liquid is above 9, CO 2 The absorption liquid is conveyed to a second spraying layer after impurities are removed by an impurity removing system; when CO is input into the first PH sorting system 2 When the pH of the absorption liquid is less than 9, the absorption liquid is conveyed to the absorbent for regeneration and CO 2 And (4) analyzing the system.
Preferably, the CO is 2 A plurality of second packing layers are arranged in the absorption region, a dividing wall type heat exchanger is arranged between any two adjacent second packing layers and is used for reducing and controlling CO 2 The reaction temperature in the absorption zone.
Preferably, the dividing wall type heat exchanger is used for controlling CO 2 The reaction temperature in the absorption zone is in the range of 38-42 ℃.
Preferably, the heat absorbed by the dividing wall type heat exchanger is used for heating the absorbent for regeneration and CO 2 And (5) analyzing the system.
Preferably, a top cap is arranged above the auxiliary channel, and a gap through which the airflow can pass is formed between the top cap and the outlet of the auxiliary channel.
Preferably, the SO 2 A plurality of first packing layers are arranged in the absorption region, and the first spraying layer is arranged above the first packing layer at the top.
Preferably, the pretreatment bell mouth further comprises a pretreatment alkali liquor injection device, the pretreatment alkali liquor injection device is provided with an alkali liquor batching and storing device and a conveying system, and the alkali liquor batching and storing device provides alkali liquor for the pretreatment alkali liquor injection device through the conveying system.
Preferably, the large-diameter end of the pretreatment bell mouth is connected with a sulfur-carbon integrated removal tower, the bottom of the pretreatment bell mouth is provided with an inclined plate, and the output end of the pretreatment bell mouth is also provided with a flow guide plate for flow equalization.
The invention has the beneficial effects that: the invention is suitable for low-sulfur coal, can economically and efficiently realize the integrated removal of sulfur and carbon, and realizes SO in the same tower body 2 And CO 2 The efficiency of the high-efficiency removal can reach more than 99 percent and 90 percent respectively, and the high-efficiency removal method is compared with the prior conventional complex processCompared with the prior art, 2-3 tower bodies are combined into a composite tower body, and the composite tower body is divided in the tower, compact in arrangement, small in occupied area and more suitable for large-scale engineering popularization.
The features and advantages of the present invention will be described in detail by embodiments in conjunction with the accompanying drawings.
[ description of the drawings ]
FIG. 1 is a schematic structural diagram of a sulfur-carbon synergistic integrated wet removal device of the present invention;
FIG. 2 is a schematic diagram of an embodiment 1 of the sulfur-carbon synergistic integrated wet removal device of the present invention.
[ detailed description ] embodiments
Referring to fig. 1, the invention relates to a sulfur and carbon cooperative integrated wet removal device, which comprises a pretreatment bell mouth 1, a sulfur and carbon integrated removal tower 2, absorbent regeneration and CO 2 Analysis System 3, absorbent regeneration and SO 2 The output end of the pretreatment bell mouth 1 is connected with the inlet of the sulfur-carbon integrated removing tower 2, and the sulfur-carbon integrated removing tower 2 is sequentially provided with SO from bottom to top 2 Absorption zone 21, CO 2 Absorption zone 22, demisting system 23, the SO 2 Absorption zone 21, the CO 2 A plurality of first spraying layers 26 and second spraying layers 28 are respectively arranged in the absorption zone 22, and the SO 2 Absorption zone 21, CO 2 The bottom of the absorption zone 22 is respectively provided with a first absorption liquid collecting system 24 and a second absorption liquid collecting system 25, and the second absorption liquid collecting system 25 is provided with an auxiliary channel 250 for airflow to pass through; the output end of the first absorption liquid collecting system 24 is connected to the absorbent regeneration and SO respectively after being shunted by the first PH sorting system 2 The analysis system 4 and the first spraying layer 26; the output end of the second absorption liquid collecting system 25 is connected to the absorbent regeneration and CO respectively after being shunted by the second PH sorting system 2 Analytic system 3, second spray level 28 (not shown).
Further, an output end of the first PH sorting system is connected to a first impurity removing system (not shown), and then is connected to the first spraying layer 26, and the first PH sorting system is used for collecting the SO output by the first absorption liquid collecting system 24 2 Shunting the absorption liquid according to the pH value; when the SO is input into the first PH sorting system 2 SO when the pH of the absorption liquid is above 4.5 2 The absorption liquid is conveyed to the first spraying layer 26 after impurities are removed by the impurity removing system; when the SO is input into the first PH sorting system 2 When the pH value of the absorption liquid is less than 4.5, the absorption liquid is conveyed to the absorbent for regeneration and SO 2 And an analysis system 4.
Further, an output end of the second PH sorting system is connected to a second impurity removing system (not shown in the figure) and then connected to the second spraying layer 28, and the second PH sorting system is used for collecting CO output by the second absorption liquid collecting system 25 2 Shunting the absorption liquid according to the pH value; when CO is input into the second PH sorting system 2 When the pH of the absorption liquid is above 9, CO 2 The absorption liquid is conveyed to the second spraying layer 28 after impurities are removed by the impurity removing system; when CO is input into the first PH sorting system 2 When the pH of the absorption liquid is less than 9, the absorption liquid is conveyed to the absorbent for regeneration and CO 2 And an analysis system 3.
Further, the CO is 2 A plurality of second packing layers are arranged in the absorption zone 22, a dividing wall type heat exchanger 27 is arranged between any two adjacent second packing layers, and the dividing wall type heat exchanger 27 is used for reducing and controlling CO 2 The reaction temperature of the absorption zone 22. In this embodiment, the second packing layer is three layers, and the second spraying layer 28 is two layers, which are respectively disposed above the two first packing layers above. The dividing wall type heat exchanger 27 is used for controlling CO 2 The reaction temperature in the absorption zone 22 is in the range of 38-42 deg.c. The heat absorbed by the dividing wall type heat exchanger 27 is used for heating the absorbent for regeneration and CO 2 Analysis of CO in System 3 2 And (4) an analytical tower.
Further, a top cap is arranged above the auxiliary channel 250, and a gap through which the airflow can pass is formed between the top cap and the outlet of the auxiliary channel 250.
Further, the SO 2 A plurality of first packing layers are arranged in the absorption region 21, and the first spraying layer 26 is arranged above the first packing layer at the top.
Further, the pretreatment horn mouth 1 further comprises a pretreatment alkali liquor injection device 11, the pretreatment alkali liquor injection device 11 is provided with an alkali liquor batching and storing device and a conveying system, and the alkali liquor batching and storing device provides alkali liquor for the pretreatment alkali liquor injection device 11 through the conveying system. In this embodiment, the major diameter end of the pretreatment bell mouth 1 is connected with the sulfur-carbon integrated removal tower 2, the bottom of the pretreatment bell mouth 1 is provided with an inclined plate 12, and the output end of the pretreatment bell mouth 1 is also provided with a flow guide plate for flow equalization.
Furthermore, the defogging system 23 adopts a folded plate turbulence defogging and electric defogging coupled synergistic defogging.
Further, absorbent regeneration and CO 2 The analysis system 3 includes CO 2 The desorption tower 30, the first heater, the compression and purification device and the like are heated by the first heater and enter the CO 2 The rich liquid in the desorption tower, and CO is desorbed from the heated rich liquid 2 Hetero-containing CO 2 The gas is converted into industrial grade or food grade CO after passing through a compression purification device 2 . Specifically, referring to FIG. 2, in example 1, CO 2 The rich solution with saturated absorption is separated by a second PH separation system, and the low PH rich solution enters an absorbent to regenerate CO 2 The high pH rich solution is sprayed into the CO of the sulfur-carbon integrated removal tower 2 again 2 The absorption zone 22 is recycled and connected to the second spray layer 28 in two ways for spraying. Low pH rich solution into CO 2 The desorption tower is cooled through a heat exchanger arranged in the second PH sorting system after being heated and regenerated, and then is connected to a second spraying layer 28 for circular spraying. CO 2 2 The desorption tower is heated by a steam heater, and two steam heaters are arranged for ensuring the heating effect.
Further, absorbent regeneration and SO 2 The analysis system 4 includes an SO 2 An analytical tower, a second heater, and SO 2 A product or fertilizer preparation device and the like. Heating the entering SO by a second heater 2 The rich liquid of the desorption tower, the heated rich liquid is desorbed to obtain SO 2 Of hetero-containing SO 2 The gas is changed into SO after passing through relevant devices 2 Products or fertilizers, etc. Specifically, referring to FIG. 2, in example 1, SO 2 The rich solution with saturated absorption is separated by a first PH separation system, and the low PH rich solution enters an absorbent to regenerate SO 2 The high PH rich solution is connected to the first spraying layer 26 again and sprayed into the SO of the sulfur-carbon integrated removal tower 2 2 The absorption zone 21 is recycled. Introducing the low-pH rich solution into an absorbent to regenerate SO 2 The desorption tower is cooled through a heat exchanger arranged in the first PH sorting system after being heated and regenerated, and then is connected to the first spraying layer 26 for circular spraying. SO 2 The desorption column is heated by a steam heater.
The working process of the invention is as follows:
the alkali liquor is pre-sprayed into the pre-treatment bell mouth 1 by the pre-treatment alkali liquor spraying device 11 and has SO 2 And a dust removal function, wherein the absorption liquid flows to the bottom of the integrated absorption tower along with the bottom inclined plate 12 to be collected, and an air flow distribution and backflow plate is additionally arranged in the bell mouth to ensure that the air flow entering the sulfur and carbon integrated removal tower 2 is uniformly distributed.
Two large areas SO in integrated absorption tower 2 Absorption zone 21, CO 2 An absorption zone 22 in which the upper CO 2 The absorption zone 22 comprises three layers of second packing layers, two layers of dividing wall type heat exchangers 27 and two layers of second spraying layers 28. Two second spray levels 28 for flue gas and CO 2 The absorption liquid is fully mixed, the dividing wall type heat exchanger 27 is used for reducing and controlling the reaction at the optimal temperature to be exothermic reaction, the optimal temperature is about 40 ℃, and the absorbed heat can be used for heating absorbent regeneration and CO 2 Analysis of CO in System 3 2 The second packing layer of the desorption tower can make CO 2 The retention time of the absorption liquid in the tower is enhanced, and the absorption effect is enhanced; CO 2 2 The absorption zone 22 primarily absorbs CO 2 But also small amounts of SO 2 Is further absorbed. Lower SO 2 The absorption zone 21 comprises 2 first filler layers, a first spray layer 26, which is mainly for absorbing SO 2 However, since part of the spray absorption liquid is branched from the upper rich liquid, part of the spray absorption liquid may also contain CO 2 Is displaced to remove SO 2 The back gas enters the upper part of the tower through the middle top cap.
CO 2 The absorption liquid is collected by the second absorption liquid collecting system 25 and then is firstly shunted by the second PH sorting system, most of the absorption liquid with PH of more than 9 enters the second impurity removing system, and the impurities are discharged and then respectively enter the upper two layersA second spray level 28, a small portion entering the lower SO 2 Absorption zone 21, incoming absorbent regeneration and CO at pH less than 9 2 The analysis system 3 can prepare over 99.9 percent of CO after heating analysis and concentration purification 2 And (5) producing the product.
SO 2 The absorption liquid is collected by the first absorption liquid collecting system 24 and then is firstly shunted by the first PH sorting system, the absorption liquid with the PH higher than 4.5 enters the first impurity removing system, the impurities are discharged and then enter the first spraying layer 26, and the absorption liquid with the PH lower than 4.5 enters the absorbent regeneration and SO separation system 2 The analysis system 4 can prepare more than 99.9 percent of SO after heating analysis, concentration and purification 2 The product is reacted with ammonia gas to prepare fertilizer.
The above embodiments are illustrative of the present invention, and are not intended to limit the present invention, and any simple modifications of the present invention are within the scope of the present invention.
Claims (10)
1. A sulphur carbon is in coordination with integrative wet process desorption device which characterized in that: comprises a pretreatment bell mouth (1), a sulfur-carbon integrated removing tower (2), absorbent regeneration and CO 2 Analysis System (3), absorbent regeneration and SO 2 The output end of the pretreatment bell mouth (1) is connected to the inlet of the sulfur and carbon integrated removing tower (2), and the sulfur and carbon integrated removing tower (2) is sequentially provided with SO from bottom to top 2 Absorption zone (21), CO 2 An absorption zone (22), a demisting system (23), the SO 2 An absorption zone (21), the CO 2 A plurality of first spraying layers (26) and second spraying layers (28) are respectively arranged in the absorption area (22), and the SO 2 Absorption zone (21), CO 2 A first absorption liquid collecting system (24) and a second absorption liquid collecting system (25) are respectively arranged at the bottom of the absorption area (22), and an auxiliary channel (250) for air flow to pass through is arranged on the second absorption liquid collecting system (25); the output end of the first absorption liquid collecting system (24) is respectively connected with the absorbent regeneration and SO after being shunted by the first PH sorting system 2 A resolution system (4), the first spray layer (26); the output end of the second absorption liquid collecting system (25) is respectively connected with the absorbent regeneration and the CO after being shunted by a second PH sorting system 2 An analysis system (3) and a second spray layer (28).
2. The integrated sulfur-carbon synergy wet removal device according to claim 1, characterized in that: one output end of the first PH sorting system is connected with the first impurity removing system and then connected to the first spraying layer (26), and the first PH sorting system is used for collecting SO output by the first absorption liquid collecting system (24) 2 Shunting the absorption liquid according to the pH value; when the SO is input into the first PH sorting system 2 SO when the pH of the absorption liquid is above 4.5 2 The absorption liquid is conveyed to a first spraying layer (26) after impurities are removed by an impurity removal system; when the SO is input into the first PH sorting system 2 When the pH value of the absorption liquid is less than 4.5, the absorption liquid is conveyed to the absorbent for regeneration and SO 2 An analysis system (4).
3. The integrated sulfur and carbon cooperative wet removal device as claimed in claim 1, wherein: one output end of the second PH sorting system is connected with the second impurity removal system and then is connected with the second spraying layer (28), and the second PH sorting system is used for collecting CO output by the second absorption liquid collection system (25) 2 Shunting the absorption liquid according to the pH value; when CO is input to the second PH sorting system 2 When the pH of the absorption liquid is above 9, CO 2 The absorption liquid is conveyed to a second spraying layer (28) after impurities are removed by an impurity removal system; when CO is input into the first PH sorting system 2 When the pH of the absorption liquid is less than 9, the absorption liquid is conveyed to the absorbent for regeneration and CO 2 An analysis system (3).
4. The integrated sulfur and carbon cooperative wet removal device as claimed in claim 1, wherein: the CO is 2 A plurality of second packing layers are arranged in the absorption area (22), a dividing wall type heat exchanger (27) is arranged between any two adjacent second packing layers, and the dividing wall type heat exchanger (27) is used for reducing and controlling CO 2 The reaction temperature of the absorption zone (22).
5. The integrated sulfur and carbon removal device of claim 4,the method is characterized in that: the dividing wall type heat exchanger (27) is used for controlling CO 2 The reaction temperature of the absorption zone (22) is in the range of 38-42 ℃.
6. The integrated sulfur and carbon cooperative wet removal device according to claim 4, wherein: the heat absorbed by the dividing wall type heat exchanger (27) is used for heating the absorbent for regeneration and CO 2 An analysis system (3).
7. The integrated sulfur and carbon cooperative wet removal device as claimed in claim 1, wherein: and a top cap is arranged above the auxiliary channel (250), and a gap through which air flow can pass is formed between the top cap and the outlet of the auxiliary channel (250).
8. The integrated sulfur and carbon cooperative wet removal device as claimed in claim 1, wherein: the SO 2 A plurality of first packing layers are arranged in the absorption region (21), and the first spraying layer (26) is arranged above the first packing layer at the top.
9. The integrated sulfur and carbon cooperative wet removal device as claimed in claim 1, wherein: the pretreatment horn mouth (1) further comprises a pretreatment alkali liquor injection device (11), the pretreatment alkali liquor injection device (11) is provided with an alkali liquor batching and storing device and a conveying system, and the alkali liquor batching and storing device provides alkali liquor for the pretreatment alkali liquor injection device (11) through the conveying system.
10. The integrated sulfur and carbon cooperative wet removal device as claimed in claim 1, wherein: the large-diameter end of the pretreatment horn mouth (1) is connected with a sulfur-carbon integrated removal tower (2), the bottom of the pretreatment horn mouth (1) is provided with an inclined plate (12), and the output end of the pretreatment horn mouth (1) is also provided with a flow guide plate for flow equalization.
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| CN202210649906.0A CN114939331A (en) | 2022-06-09 | 2022-06-09 | Sulfur-carbon synergetic integrated wet-process removal device |
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| CN202210649906.0A CN114939331A (en) | 2022-06-09 | 2022-06-09 | Sulfur-carbon synergetic integrated wet-process removal device |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0947631A (en) * | 1995-08-09 | 1997-02-18 | Babcock Hitachi Kk | Wet type flue gas desulfurization facility |
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