CN202006081U - System for trapping and absorbing sulfur dioxide and carbon dioxide at normal pressure through ammonia process - Google Patents

System for trapping and absorbing sulfur dioxide and carbon dioxide at normal pressure through ammonia process Download PDF

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Publication number
CN202006081U
CN202006081U CN2011200404524U CN201120040452U CN202006081U CN 202006081 U CN202006081 U CN 202006081U CN 2011200404524 U CN2011200404524 U CN 2011200404524U CN 201120040452 U CN201120040452 U CN 201120040452U CN 202006081 U CN202006081 U CN 202006081U
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China
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pipeline
tank
import
pump
carbon dioxide
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CN2011200404524U
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Chinese (zh)
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徐敬尧
陈林
张明旭
韩松
苏传好
闵凡飞
李寒旭
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安徽淮化股份有限公司
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Priority claimed from PCT/CN2012/071026 external-priority patent/WO2012109964A1/en

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    • Y02A50/2342

Abstract

The utility model relates to a system for trapping and absorbing sulfur dioxide and carbon dioxide at normal pressure through an ammonia process, which comprises a dilute ammonia water supply device and the like. The dilute ammonia water supply device is respectively connected with a sulfur dioxide absorbing device and a carbon dioxide absorbing device through pipelines. A draught fan is connected with a heat exchanger through a pipeline. The heat exchanger is connected with the sulfur dioxide absorbing device through a pipeline. A sulfur dioxide absorbing tower exhaust pipe is connected with a carbon dioxide absorbing tower. A first cooling device and a second cooling device in the sulfur dioxide absorbing tower and the carbon dioxide absorbing tower share a cooling water inlet pipe and a cooling water outlet pipe. The sulfur dioxide absorbing device and the carbon dioxide absorbing device are respectively replenished through concentrated ammonia water in a high-concentration ammonia water storage tank. The sulfur dioxide absorbing device and the carbon dioxide absorbing device respectively pump solution in the respective absorbing towers to the heat exchanger for cooling and to a crystallization tank for crystallization through pumps. Solid and liquid are separated through a centrifuge. The liquid is continuously circulated in the system. The system has the advantages of high desulphurization and carbon reduction efficiency, simple process flow, simplified system structure and low investment and operating cost.

Description

The ammonia process normal pressure captures and absorbs sulfur dioxide and carbon dioxide system

Technical field

The utility model relates to coal-fired plant flue gas purification and sulfur dioxide, carbon dioxide discharge-reduction field, relates to a kind of ammonia process normal pressure specifically and captures and absorb sulfur dioxide and carbon dioxide system.

Background technology

At present, the reduction of discharging of sulfur dioxide and carbon dioxide generally is separately to carry out, it is first desulfurization decarburization again, flue gas desulfurization technique is mainly with the limestone-gypsum wet method, the rotating spraying semidry method, in-furnace calcium spraying afterbody humidification activation, sea water desulfuration, the electricity bundle desulfurization, flue gas circulating fluidized bed desulfurization etc. are main, wherein the wet type limestone-based process is the tail flue gas desulfur technology that is most widely used in the world now, this technology is to absorb sulfur dioxide in the flue gas with lime slurry or lime in the absorption tower, producing thing is calcium sulfite and calcium sulfate, its desulfuration efficiency is 75%-95%, its subject matter is that the solubility of absorbent (lime or lime stone) is little, utilization rate is low, the ash quantity of slag is big, cause thus fouling and obstruction easily take place in desulphurization plant and the pipeline, and produce thing and also can cause secondary pollution.Dry desulfurization and semi-dry desulphurization are owing to the reason of absorbent with flue gas weak point time of contact, desulfuration efficiency is generally between 50%-75%, eliminating efficiency is low, and exist solid pollutant secondary pollution problem absorption method to mainly contain Wellman-Lord method, activated carbon method, ammonia process etc. equally, the Wellman-Lord method uses sodium sulfite as absorbent, desulfuration efficiency can reach 95%, but the investment of this technology and operating cost are all higher; Though the activated carbon method desulfuration efficiency can reach 98%, this complex process, technical difficulty are big and the active carbon consumption is big; Ammonia process of desulfurization efficient is generally between 95%-99%, desulfurization product can be directly when the fertilizer use, do not produce waste water and other refuses, have the incomparable advantage of other technologies, ammonia loses higher and problem that directly cause desulfuration efficiency to reduce in the tail gas but this technology often exists.Subtract carbon technique both at home and abroad and mainly contain absorption process, absorption method, membrane separation process and seal method etc. up for safekeeping, all have certain weak point.

The utility model content

The purpose of this utility model provides a kind of ammonia process normal pressure and captures and absorb sulfur dioxide and carbon dioxide system, and its desulfurization subtracts the carbon efficiencies height, and technological process is simple, system architecture simplification, investment and operating cost are cheap.

In order to realize such scheme, technical solution of the present utility model is: a kind of ammonia process normal pressure captures and absorbs sulfur dioxide and carbon dioxide system, comprising the weak aqua ammonia feedway, air-introduced machine, first heat exchanger, high concentration ammoniacal liquor storage tank, first, two pumps, apparatus for absorbing SO 2 and absorption unit of dioxide carbon, described apparatus for absorbing SO 2 comprises the sulfur dioxide absorption tower of normal pressure, second heat exchanger, the sulfur dioxide crystallization tank, the ammonium sulfate product centrifuge, first mother liquor tank and the 5th, six pumps, described sulfur dioxide absorption tower comprises first tank body, on in first cooling device in the tank body and the tank body, the middle part be provided with respectively first, two spray equipments, described absorption unit of dioxide carbon comprises the carbon dioxide absorption tower of normal pressure, the 3rd heat exchanger, the carbon dioxide crystallization tank, carbonic hydroammonium product centrifuge, second mother liquor tank and the 7th, eight pumps, described carbon dioxide absorption tower comprises second tank body, on in second cooling device in the tank body and the tank body, the middle part be provided with respectively the 3rd, four spray equipments, described weak aqua ammonia feedway by pipeline respectively with described first, three spray equipments connect, described air-introduced machine is connected by the air inlet of pipeline with first heat exchanger, the exhaust outlet of described first heat exchanger stretches into the described first tank inner chamber bottom by pipeline, described first tank base is connected by the import of pipeline with the 5th pump, described the 5th delivery side of pump is connected by the import of pipeline with second heat exchanger, the outlet of described second heat exchanger is connected by the import of pipeline with the sulfur dioxide crystallization tank, the outlet of described sulfur dioxide crystallization tank is connected by the import of pipeline with the ammonium sulfate product centrifuge, the outlet of described ammonium sulfate product centrifuge is connected by the import of pipeline with first mother liquor tank, the outlet of described first mother liquor tank is connected with the 6th pump by pipeline, described the 6th pump is connected with described second spray equipment by pipeline, the described the 5th, connect first pipeline between the import of six pumps, described high concentration ammoniacal liquor storage tank by pipeline respectively with first, the import of two pumps connects, described first, two delivery side of pump are respectively with second, four spray equipments connect, the described first tank body top is communicated with the second tank inner chamber bottom by blast pipe, described first, the cooling water inlet pipe of the cooling water inlet pipe of two cooling devices and first heat exchanger links together, described first, the cooling water outlet pipe of the cooling water outlet pipe of two cooling devices and first heat exchanger links together, be respectively arranged with first on the described cooling water inlet pipe, two control valves, described second tank base is connected by the import of pipeline with the 7th pump, described the 7th delivery side of pump is connected by the import of pipeline with the 3rd heat exchanger, the outlet siphunculus road of described the 3rd heat exchanger is connected with the import of carbon dioxide crystallization tank, the outlet of described carbon dioxide crystallization tank is connected by the import of pipeline with carbonic hydroammonium product centrifuge, the outlet of described carbonic hydroammonium product centrifuge is connected by the import of pipeline with second mother liquor tank, the outlet of described second mother liquor tank is connected with the 8th pump by pipeline, described the 8th pump is connected the described the 7th by pipeline with described the 4th spray equipment, connect second pipeline between the import of eight pumps.

The utility model ammonia process normal pressure captures and absorbs sulfur dioxide and carbon dioxide system, wherein said weak aqua ammonia feedway is made up of weak aqua ammonia storage tank and third and fourth pump, described weak aqua ammonia storage tank is connected with the import of third and fourth pump respectively by pipeline, described third and fourth delivery side of pump is connected with described first and third spray equipment respectively, is respectively arranged with valve on the described pipeline.

After adopting such scheme, the utility model ammonia process normal pressure capture to absorb sulfur dioxide and carbon dioxide system makes sulfur dioxide in coal-burning power plant's flue gas by adopting sulfur dioxide absorption tower and carbon dioxide absorption tower, carbon dioxide generates ammonium sulfate and ammonium bicarbonate soln respectively with the reverse full contact reaction of weak aqua ammonia absorbent solution respectively, and the unsaturated ammonium sulfate of applying in a flexible way and producing, ammonium bicarbonate soln and increased benefit high strength ammonia water conservancy project preface and sulfur dioxide absorption tower, establish cooling device in the carbon dioxide absorption tower, the desired production status of this technology of control that can be good, make sulfur dioxide and carbon dioxide in coal-burning power plant's flue gas obtain good capture absorption, desulfurization subtracts the carbon efficiencies height, sulfur dioxide and discharge of carbon dioxide greenhouse gas have been reduced, ammonium sulfate and ammonium bicarbonate fertilizer have been produced simultaneously, unique process pipelines design makes the trapping system flexible operation, reduced the power consumption when system moves, simultaneously more effectively improved sulfur dioxide of flue gases to the coal-burning power plant, the capture absorbability of carbon dioxide, this technological process is simplified, system architecture is simplified, investment and operating cost are cheap.

Description of drawings

Fig. 1 is that the utility model ammonia process normal pressure captures absorption sulfur dioxide and carbon dioxide system structural representation.

The specific embodiment

As shown in Figure 1, the utility model ammonia process normal pressure capture absorption sulfur dioxide and carbon dioxide system structure comprise weak aqua ammonia feedway 1, air-introduced machine 2, first heat exchanger 3, high concentration ammoniacal liquor storage tank 4, first pump 5, second pump 6, apparatus for absorbing SO 27 and absorption unit of dioxide carbon 8;

Weak aqua ammonia feedway 1 is made up of weak aqua ammonia storage tank 11, the 3rd pump 12 and the 4th pump 13, and weak aqua ammonia storage tank 11 is connected with the import of the 3rd pump 12 and the 4th pump 13 respectively by pipeline, is respectively arranged with valve 30 and valve 40 on the pipeline;

Apparatus for absorbing SO 27 comprises sulfur dioxide absorption tower 71, second heat exchanger 72, sulfur dioxide crystallization tank 73, ammonium sulfate product centrifuge 74, first mother liquor tank 75, the 5th pump 76 and the 6th pump 77 of normal pressure, sulfur dioxide absorption tower 71 comprise in first cooling device 712 in first tank body 711, tank body and the tank body go up, first shower device 713 that the middle part is provided with respectively and the outlet of second spray equipment, 714, the three pumps 12 be connected with first spray equipment 713 by pipeline;

Absorption unit of dioxide carbon 8 comprises carbon dioxide absorption tower 81, the 3rd heat exchanger 82, carbon dioxide crystallization tank 83, carbonic hydroammonium product centrifuge 84, second mother liquor tank 85 and the 7th pump 86 and the 8th pump 87 of normal pressure, carbon dioxide absorption tower 81 comprise in second cooling device 812 in second tank body 811, tank body and the tank body go up, the 3rd spray equipment 813 that the middle part is provided with respectively and the outlet of the 4th spray equipment 814, the four pumps 13 be connected with the 3rd spray equipment 813 by pipeline;

Air-introduced machine 2 is connected by the air inlet of pipeline with first heat exchanger 3, the exhaust outlet of first heat exchanger 3 stretches into first tank body, 711 inner chamber bottoms by pipeline, first tank body, 711 bottoms are connected by the import of pipeline with the 5th pump 76, the outlet of the 5th pump 76 is connected by the import of pipeline with second heat exchanger 72, the outlet of second heat exchanger 72 is connected by the import of pipeline with sulfur dioxide crystallization tank 73, the outlet of sulfur dioxide crystallization tank 73 is connected by the import of pipeline with ammonium sulfate product centrifuge 74, the outlet of ammonium sulfate product centrifuge 74 is connected by the import of pipeline with first mother liquor tank 75, the outlet of first mother liquor tank 75 is connected with the 6th pump 77 by pipeline, the 6th pump 77 is connected with second spray equipment 714 by pipeline, the 5th pump 76, connect first pipeline 9 between the import of the 6th pump 77, high concentration ammoniacal liquor storage tank 4 is connected with the import of first pump 5 and second pump 6 respectively by pipeline, the outlet of first pump 5 and second pump 6 is connected with the 4th spray equipment 814 with second spray equipment 714 respectively, first tank body, 711 tops are communicated with second tank body, 811 inner chamber bottoms by blast pipe 7111, first cooling device 712, the cooling water inlet pipe of the cooling water inlet pipe of second cooling device 812 and first heat exchanger 3 links together, first cooling device 712, the cooling water outlet pipe of the cooling water outlet pipe of second cooling device 812 and first heat exchanger 3 links together, be respectively arranged with first control valve 10 and second control valve 50 on the cooling water inlet pipe, second tank body, 811 bottoms are connected by the import of pipeline with the 7th pump 86, the outlet of the 7th pump 86 is connected by the import of pipeline with the 3rd heat exchanger 82, the outlet siphunculus road of the 3rd heat exchanger 82 is connected with the import of carbon dioxide crystallization tank 83, the outlet of carbon dioxide crystallization tank 83 is connected by the import of pipeline with carbonic hydroammonium product centrifuge 84, the outlet of carbonic hydroammonium product centrifuge 84 is connected by the import of pipeline with second mother liquor tank 85, the outlet of second mother liquor tank 85 is connected with the 8th pump 87 by pipeline, the 8th pump 87 is connected with the 4th spray equipment 814 by pipeline, connects second pipeline 20 between the import of the 7th pump 86 and the 8th pump 87.

Adopt the processing step of said system capture absorption sulfur dioxide and carbon dioxide as follows:

(1) will through coal-burning power plant's flue gas of dust removal process in air-introduced machine 2 suction first heat exchanger 3, reach the required temperature of production technology by 3 coolings of first heat exchanger;

(2) will enter through the bottom of the coal-burning power plant's flue gas after dedusting and the cooling processing from sulfur dioxide absorption tower 71, the weak aqua ammonia absorbent solution that can capture in the weak aqua ammonia storage tank 11 that absorbs sulfur dioxide sprays downwards by first spray equipment 713 that the 3rd pump 12 pumps in the sulfur dioxide absorption tower 711, reaction temperature in the sulfur dioxide absorption tower 71 is controlled between 65-80 ℃ by first cooling device 712, specifically be by controlling first control valve 10 on first cooling device, 712 water inlet pipes, control the reaction temperature of solution in the sulfur dioxide absorption tower 71 by the internal circulating load of regulating water, flue gas and the reaction of weak aqua ammonia absorbent solution counter current contacting generation gas-liquid two-phase, absorb sulfur dioxide and generated ammonium sulfate, its chemical reaction is two processes: at first the reaction of weak aqua ammonia and sulfur dioxide generates ammonium sulfite, secondly ammonium sulfite generates ammonium sulfate with the ammoniacal liquor reaction, deviates from the flue gas of sulfur dioxide and introduces in the carbon dioxide absorption tower 71 by blast pipe 7111;

(3) after the unsaturated ammonium sulfate in the sulfur dioxide absorption tower 71 reaches the requirement of technology liquid level, stop to inject the weak aqua ammonia absorbent solutions to sulfur dioxide absorption tower 71;

(4) in weak aqua ammonia absorbent solution by first spray equipment 713 on sulfur dioxide absorption tower 71 downwards during spray, ammonium sulfate in the sulfur dioxide absorption tower 71 is pumped into cooling in second heat exchanger 72 by the 5th pump 76, deliver to afterwards in the sulfur dioxide crystallization tank 73, saturated ammonium sulfate solution crystallization solid and unsaturated ammonium sulfate are together delivered to by pipeline and are carried out Separation of Solid and Liquid in the ammonium sulfate product centrifuge 74, crystalline solid ammonium sulfate fertilizer is separated, remaining unsaturated ammonium sulfate enters in first mother liquor tank 75 by pipeline, and extract in second spray equipment 714 that pumps into sulfur dioxide absorption tower 71 spray downwards out by the 6th pump 77, the unsaturated ammonium sulfate of 71 bottoms, sulfur dioxide absorption tower is by first pipeline 9, directly pump into second spray equipment, the 714 interior sprays downwards on sulfur dioxide absorption tower 71 by the 6th pump 77 on first pipeline 9, with the weak aqua ammonia absorbent solution that before sprayed into together or separately and the sulfur dioxide gas in the flue gas in the sulfur dioxide absorption tower 71 reverse absorption reaction takes place, reach the absorption of sulfur dioxide and make ammonium sulfate from the unsaturated saturated solution that becomes;

(5) from high concentration ammoniacal liquor storage tank 4, extract high concentration ammoniacal liquor out by first pump 5 and in the sulfur dioxide absorption tower 71 of finishing after the ammonium sulfate fertilizer product separates, replenish high concentration ammoniacal liquor, weak aqua ammonia absorbent solution concentration when making solution concentration in the sulfur dioxide absorption tower 71 return to beginning, promptly mass percent is between the 6%-8%;

(6) will deviate from coal-burning power plant's flue gas that sulfur dioxide treatment crosses enters from the bottom of carbon dioxide absorption tower 81, the weak aqua ammonia storage tank 11 interior weak aqua ammonia absorbent solutions that can capture absorbing carbon dioxide spray downwards by the 3rd spray equipments 813 that the 4th pump 13 pumps in the carbon dioxide absorption tower 81, reaction temperature in the carbon dioxide absorption tower 81 is controlled between 40-50 ℃ by second cooling device 812, specifically be by controlling second control valve 50 on second cooling device, 812 water inlet pipes, control the reaction temperature of solution in the carbon dioxide absorption tower 81 by the internal circulating load of regulating water, flue gas and the reaction of weak aqua ammonia absorbent solution counter current contacting generation gas-liquid two-phase, absorbed carbon dioxide and generated ammonium bicarbonate soln, deviate from the flue gas of sulfur dioxide and carbon dioxide and discharge through the pipeline at carbon dioxide absorption tower 81 tops;

(7) after the unsaturated carbonic acid hydrogen ammonium salt solution in the carbon dioxide absorption tower 81 reaches the requirement of technology liquid level, stop in carbon dioxide absorption tower 81, to inject weak aqua ammonia absorbent solution;

(8) in weak aqua ammonia absorbent solution by the 3rd spray equipment 813 of carbon dioxide absorption tower 81 downwards during spray, ammonium bicarbonate soln in the carbon dioxide absorption tower 81 is pumped into cooling in the 3rd heat exchanger 82 by the 7th pump 86, deliver to afterwards in the carbon dioxide crystallization tank 83, unsaturated carbonate hydrogen ammonium salt solution crystalline solid and unsaturated carbonic acid hydrogen ammonium salt solution are together delivered in the carbonic hydroammonium product centrifuge 84 by pipeline and are carried out Separation of Solid and Liquid, the crystalline solid ammonium bicarbonate fertilizer is separated, remaining unsaturated carbonic acid hydrogen ammonium salt solution enters in second mother liquor tank 85 by pipeline, and extract in the 4th spray equipment 814 that pumps into carbon dioxide absorption tower 81 spray downwards out by the 8th pump 87, the unsaturated carbonic acid hydrogen ammonium salt solution of carbon dioxide absorption tower 81 bottoms is by second pipeline 20, directly pump into the 4th spray equipment 814 interior sprays downwards of carbon dioxide absorption tower 81 by the 8th pump 87 on second pipeline 20, with the weak aqua ammonia absorbent solution that before sprayed into together or separately and the carbon dioxide in the flue gas in the carbon dioxide absorption tower 81 reverse absorption reaction takes place, reach the absorption of carbon dioxide and make ammonium bicarbonate soln from the unsaturated saturated solution that becomes;

(9) from high concentration ammoniacal liquor storage tank 4, extract high concentration ammoniacal liquor out by second pump 6 and in the carbon dioxide absorption tower of finishing after the ammonium bicarbonate fertilizer product separates 81, replenish high concentration ammoniacal liquor, weak aqua ammonia absorbent solution concentration when making solution concentration in the carbon dioxide absorption tower 81 return to beginning, promptly mass percent is between the 6%-8%;

(10) circulation above-mentioned steps.

The utility model ammonia process normal pressure capture to absorb sulfur dioxide and carbon dioxide system makes sulfur dioxide in coal-burning power plant's flue gas by adopting sulfur dioxide absorption tower 71 and carbon dioxide absorption tower 81, carbon dioxide generates ammonium sulfate and ammonium bicarbonate soln respectively with the reverse full contact reaction of weak aqua ammonia absorbent solution respectively, and the unsaturated ammonium sulfate of applying in a flexible way and producing, ammonium bicarbonate soln and increased benefit high strength ammonia water conservancy project preface and sulfur dioxide absorption tower 71, establish first cooling device 712 and second cooling device 812 in the carbon dioxide absorption tower 81 respectively, the desired production status of this technology of control that can be good, make sulfur dioxide and carbon dioxide in coal-burning power plant's flue gas obtain good capture absorption, desulfurization subtracts the carbon efficiencies height, sulfur dioxide and discharge of carbon dioxide greenhouse gas have been reduced, ammonium sulfate and ammonium bicarbonate fertilizer have been produced simultaneously, unique process pipelines design makes the trapping system flexible operation, reduced the power consumption when system moves, simultaneously more effectively improved sulfur dioxide of flue gases to the coal-burning power plant, the capture absorbability of carbon dioxide, this technological process is simplified, system architecture is simplified, investment and operating cost are cheap.

The above embodiment is described preferred implementation of the present utility model; be not that scope of the present utility model is limited; under the prerequisite that does not break away from the utility model design spirit; various distortion and improvement that the common engineers and technicians in this area make the technical solution of the utility model all should fall in the definite protection domain of claims of the present utility model.

Claims (2)

1. an ammonia process normal pressure captures and absorbs sulfur dioxide and carbon dioxide system, it is characterized in that: comprise weak aqua ammonia feedway (1), air-introduced machine (2), first heat exchanger (3), high concentration ammoniacal liquor storage tank (4), first, two pumps (5,6), apparatus for absorbing SO 2 (7) and absorption unit of dioxide carbon (8), described apparatus for absorbing SO 2 (7) comprises the sulfur dioxide absorption tower (71) of normal pressure, second heat exchanger (72), sulfur dioxide crystallization tank (73), ammonium sulfate product centrifuge (74), first mother liquor tank (75) and the 5th, six pumps (76,77), described sulfur dioxide absorption tower (71) comprises first tank body (711), on in first cooling device (712) in the tank body and the tank body, the middle part be provided with respectively first, two spray equipments (713,714), described absorption unit of dioxide carbon (8) comprises the carbon dioxide absorption tower (81) of normal pressure, the 3rd heat exchanger (82), carbon dioxide crystallization tank (83), carbonic hydroammonium product centrifuge (84), second mother liquor tank (85) and the 7th, eight pumps (86,87), described carbon dioxide absorption tower (81) comprises second tank body (811), on in second cooling device (812) in the tank body and the tank body, the middle part be provided with respectively the 3rd, four spray equipments (813,814), described weak aqua ammonia feedway (1) by pipeline respectively with described first, three spray equipments (713,813) connect, described air-introduced machine (2) is connected by the air inlet of pipeline with first heat exchanger (3), the exhaust outlet of described first heat exchanger (3) stretches into described first tank body (711) inner chamber bottom by pipeline, described first tank body (711) bottom is connected by the import of pipeline with the 5th pump (76), the outlet of described the 5th pump (76) is connected by the import of pipeline with second heat exchanger (72), the outlet of described second heat exchanger (72) is connected by the import of pipeline with sulfur dioxide crystallization tank (73), the outlet of described sulfur dioxide crystallization tank (73) is connected by the import of pipeline with ammonium sulfate product centrifuge (74), the outlet of described ammonium sulfate product centrifuge (74) is connected by the import of pipeline with first mother liquor tank (75), the outlet of described first mother liquor tank (75) is connected with the 6th pump (77) by pipeline, described the 6th pump (77) is connected with described second spray equipment (714) by pipeline, the described the 5th, six pumps (76,77) connect first pipeline (9) between the import, described high concentration ammoniacal liquor storage tank (4) by pipeline respectively with first, two pumps (5,6) import connects, described first, two pumps (5,6) outlet is respectively with second, four spray equipments (714,814) connect, described first tank body (711) top is communicated with second tank body (811) inner chamber bottom by blast pipe (7111), described first, two cooling devices (712, the cooling water inlet pipe of cooling water inlet pipe 812) and first heat exchanger (3) links together, described first, two cooling devices (712, the cooling water outlet pipe of cooling water outlet pipe 812) and first heat exchanger (3) links together, be respectively arranged with first on the described cooling water inlet pipe, two control valves (10,50), described second tank body (811) bottom is connected by the import of pipeline with the 7th pump (86), the outlet of described the 7th pump (86) is connected by the import of pipeline with the 3rd heat exchanger (82), the outlet siphunculus road of described the 3rd heat exchanger (82) is connected with the import of carbon dioxide crystallization tank (83), the outlet of described carbon dioxide crystallization tank (83) is connected by the import of pipeline with carbonic hydroammonium product centrifuge (84), the outlet of described carbonic hydroammonium product centrifuge (84) is connected by the import of pipeline with second mother liquor tank (85), the outlet of described second mother liquor tank (85) is connected with the 8th pump (87) by pipeline, described the 8th pump (87) is connected with described the 4th spray equipment (814) by pipeline, the described the 7th, connect second pipeline (20) between the import of eight pumps (86,87).
2. ammonia process normal pressure as claimed in claim 1 captures and absorbs sulfur dioxide and carbon dioxide system, it is characterized in that: described weak aqua ammonia feedway (1) is by weak aqua ammonia storage tank (11) and third and fourth pump (12,13) form, described weak aqua ammonia storage tank (11) connects described third and fourth pump (12 with the import of third and fourth pump (12,13) respectively by pipeline, 13) outlet respectively with described first and third spray equipment (713,813) connect, be respectively arranged with valve (30,40) on the described pipeline.
CN2011200404524U 2011-02-16 2011-02-16 System for trapping and absorbing sulfur dioxide and carbon dioxide at normal pressure through ammonia process CN202006081U (en)

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CN2011200404524U CN202006081U (en) 2011-02-16 2011-02-16 System for trapping and absorbing sulfur dioxide and carbon dioxide at normal pressure through ammonia process
PCT/CN2012/071026 WO2012109964A1 (en) 2011-02-16 2012-02-10 System and process for trapping sulfur dioxide and carbon dioxide by ammonia absorption at atmospheric pressure
US14/000,162 US8858905B2 (en) 2011-02-16 2012-02-10 System and process for trapping sulfur dioxide and carbon dioxide by ammonia absorption at atmospheric pressure

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102120137A (en) * 2011-02-16 2011-07-13 安徽淮化股份有限公司 System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method
WO2012109964A1 (en) * 2011-02-16 2012-08-23 安徽淮化股份有限公司 System and process for trapping sulfur dioxide and carbon dioxide by ammonia absorption at atmospheric pressure
CN103007719A (en) * 2013-01-16 2013-04-03 哈尔滨工业大学 Double-circulation ammonia process type smoke decarbonization device
CN104511228A (en) * 2014-12-11 2015-04-15 中国华能集团清洁能源技术研究院有限公司 Process system and method for flue gas combined desulfurization and decarburization
WO2019056858A1 (en) * 2017-09-22 2019-03-28 Jiangnan Environmental Protection Group Inc. Carbon capture

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102120137A (en) * 2011-02-16 2011-07-13 安徽淮化股份有限公司 System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method
WO2012109964A1 (en) * 2011-02-16 2012-08-23 安徽淮化股份有限公司 System and process for trapping sulfur dioxide and carbon dioxide by ammonia absorption at atmospheric pressure
US8858905B2 (en) 2011-02-16 2014-10-14 Anhui Huaihua Co. Ltd. System and process for trapping sulfur dioxide and carbon dioxide by ammonia absorption at atmospheric pressure
CN103007719A (en) * 2013-01-16 2013-04-03 哈尔滨工业大学 Double-circulation ammonia process type smoke decarbonization device
CN104511228A (en) * 2014-12-11 2015-04-15 中国华能集团清洁能源技术研究院有限公司 Process system and method for flue gas combined desulfurization and decarburization
WO2019056858A1 (en) * 2017-09-22 2019-03-28 Jiangnan Environmental Protection Group Inc. Carbon capture

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