CN102120137B - System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method - Google Patents

System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method Download PDF

Info

Publication number
CN102120137B
CN102120137B CN2011100393632A CN201110039363A CN102120137B CN 102120137 B CN102120137 B CN 102120137B CN 2011100393632 A CN2011100393632 A CN 2011100393632A CN 201110039363 A CN201110039363 A CN 201110039363A CN 102120137 B CN102120137 B CN 102120137B
Authority
CN
China
Prior art keywords
pipeline
tank
pump
import
carbon dioxide
Prior art date
Application number
CN2011100393632A
Other languages
Chinese (zh)
Other versions
CN102120137A (en
Inventor
徐敬尧
陈林
张明旭
韩松
苏传好
闵凡飞
李寒旭
Original Assignee
安徽淮化股份有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 安徽淮化股份有限公司 filed Critical 安徽淮化股份有限公司
Priority to CN2011100393632A priority Critical patent/CN102120137B/en
Publication of CN102120137A publication Critical patent/CN102120137A/en
Priority claimed from PCT/CN2012/071026 external-priority patent/WO2012109964A1/en
Application granted granted Critical
Publication of CN102120137B publication Critical patent/CN102120137B/en

Links

Classifications

    • Y02A50/2342

Abstract

The invention discloses a system and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using an ammonia method. The system comprises a diluted ammonia water supply device and the like, wherein the diluted 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, an exhaust pipe of a sulfur dioxide absorbing tower is connected with a carbon dioxide absorbing tower, a first and a second cooling devices 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 with concentrated ammonia water in a high-concentration ammonia water storage tank, and are used for pumping solutions in respective absorbing towers to the heat exchanger through pumps for cooling, the cooled solutions enter a crystallization tank for crystallization, solid and liquid are separated through a centrifugal machine, and the liquid is continuously circulated in the system. The invention has the advantages of high desulfuration carbon-reducing efficiency, simple process procedure, simplified system structure and low investment and operation cost.

Description

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

Technical field

The present invention relates to coal-fired plant flue gas purification and sulfur dioxide, carbon dioxide discharge-reduction field, relate to a kind of ammonia process normal pressure specifically and capture absorbing 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, promptly first desulfurization decarburization again; Flue gas desulfurization technique is main with limestone-gypsum wet method, rotating spraying semidry method, in-furnace calcium spraying afterbody humidification activation, sea water desulfuration, electron beam desulfurization, flue gas circulating fluidized bed desulfurization etc. mainly; Wherein the wet type limestone-based process is to use tail flue gas desulfur technology the most widely now in the world, and this technology is with lime slurry or lime sulfur dioxide in the absorption from flue gas in the absorption tower, and 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, and utilization rate is low, and the grey quantity of slag is big; Cause thus to be prone to take place fouling and obstruction 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 exists solid pollutant secondary pollution problem absorption method to mainly contain Wellman-Lord method, activated carbon method, ammonia process etc. equally, and 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.

Summary of the invention

The purpose of this invention is to provide a kind of ammonia process normal pressure and capture absorbing sulfur dioxide and carbon dioxide system, 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 invention is: a kind of ammonia process normal pressure captures absorbing sulfur dioxide and carbon dioxide system; Comprising weak aqua ammonia feedway, air-introduced machine, first heat exchanger, high concentration ammoniacal liquor storage tank, first and second pump, apparatus for absorbing SO 2 and absorption unit of dioxide carbon; Said apparatus for absorbing SO 2 comprises sulfur dioxide absorption tower, second heat exchanger, sulfur dioxide crystallization tank, ammonium sulfate product centrifuge, first mother liquor tank and the 5th, six pumps of normal pressure; Said sulfur dioxide absorption tower comprises first cooling device in first tank body, the tank body and first and second spray equipment that tank body is interior upward, the middle part is provided with respectively; Said absorption unit of dioxide carbon comprises carbon dioxide absorption tower, the 3rd heat exchanger, carbon dioxide crystallization tank, carbonic hydroammonium product centrifuge, second mother liquor tank and the 7th, eight pumps of normal pressure, and said carbon dioxide absorption tower comprises second cooling device in second tank body, the tank body and third and fourth spray equipment that tank body is interior upward, the middle part is provided with respectively, and said weak aqua ammonia feedway is connected with said first and third spray equipment respectively through pipeline; Said air-introduced machine is connected with the air inlet of first heat exchanger through pipeline; The exhaust outlet of said first heat exchanger stretches into the said first tank inner chamber bottom through pipeline, and said first tank base is connected with the import of the 5th pump through pipeline, and said the 5th delivery side of pump is connected with the import of second heat exchanger through pipeline; The outlet of said second heat exchanger is connected with the import of sulfur dioxide crystallization tank through pipeline; The outlet of said sulfur dioxide crystallization tank is connected with the import of ammonium sulfate product centrifuge through pipeline, and the outlet of said ammonium sulfate product centrifuge is connected with the import of first mother liquor tank through pipeline, and the outlet of said first mother liquor tank is connected with the 6th pump through pipeline; Said the 6th pump is connected with said second spray equipment through pipeline; Connect first pipeline between the import of said the 5th, six pumps, said high concentration ammoniacal liquor storage tank is connected with the import of first and second pump respectively through pipeline, and said first and second delivery side of pump is connected with second, four spray equipments respectively; The said first tank body top is communicated with the second tank inner chamber bottom through blast pipe; The cooling water inlet pipe of the cooling water inlet pipe of said first and second cooling device and first heat exchanger links together, and the cooling water outlet pipe of the cooling water outlet pipe of said first and second cooling device and first heat exchanger links together, and is respectively arranged with first and second control valve on the said cooling water inlet pipe; Said second tank base is connected with the import of the 7th pump through pipeline; Said the 7th delivery side of pump is connected with the import of the 3rd heat exchanger through pipeline, and the outlet siphunculus road of said the 3rd heat exchanger is connected with the import of carbon dioxide crystallization tank, and the outlet of said carbon dioxide crystallization tank is connected with the import of carbonic hydroammonium product centrifuge through pipeline; The outlet of said carbonic hydroammonium product centrifuge is connected with the import of second mother liquor tank through pipeline; The outlet of said second mother liquor tank is connected with the 8th pump through pipeline, and said the 8th pump is connected with said the 4th spray equipment through pipeline, connects second pipeline between the import of said the 7th, eight pumps.

Ammonia process normal pressure of the present invention captures absorbing 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; Said weak aqua ammonia storage tank is connected with the import of third and fourth pump respectively through pipeline; Said third and fourth delivery side of pump is connected with said first and third spray equipment respectively, is respectively arranged with valve on the said pipeline.

After adopting such scheme; Ammonia process normal pressure of the present invention captures absorbing sulfur dioxide and carbon dioxide system adopts sulfur dioxide absorption tower and carbon dioxide absorption tower to make sulfur dioxide, carbon dioxide in coal-burning power plant's flue gas generate ammonium sulfate and ammonium bicarbonate soln respectively with the reverse full contact reaction of weak aqua ammonia absorbent solution respectively; And apply in a flexible way unsaturated ammonium sulfate, the ammonium bicarbonate soln produced and increased benefit high strength ammonia water conservancy project preface and sulfur dioxide absorption tower, carbon dioxide absorption tower in establish cooling device; The desired production status of ability this technology of better controlling; Make sulfur dioxide and carbon dioxide in coal-burning power plant's flue gas obtain good capture absorption; Desulfurization subtracts the carbon efficiencies height, has reduced sulfur dioxide and discharge of carbon dioxide greenhouse gas, has produced ammonium sulfate and ammonium bicarbonate fertilizer simultaneously; Unique process pipelines design makes the trapping system flexible operation; Reduced the power consumption when system moves, the more effective capture absorbability that has improved coal-burning power plant's sulfur dioxide of flue gases, carbon dioxide of while, this technological process simplification, system architecture simplification, investment and operating cost are cheap.

Description of drawings

Fig. 1 is that ammonia process normal pressure of the present invention captures absorbing sulfur dioxide and carbon dioxide system structural representation.

The specific embodiment

As shown in Figure 1, ammonia process normal pressure of the present invention captures absorbing sulfur dioxide and carbon dioxide system structure and comprises 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 through 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 and the tank body in first tank body 711, 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 through 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 and the tank body in second tank body 811, 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 through pipeline;

Air-introduced machine 2 is connected with the air inlet of first heat exchanger 3 through pipeline; The exhaust outlet of first heat exchanger 3 stretches into first tank body, 711 inner chamber bottoms through pipeline; First tank body, 711 bottoms are connected with the import of the 5th pump 76 through pipeline; The outlet of the 5th pump 76 is connected with the import of second heat exchanger 72 through pipeline; The outlet of second heat exchanger 72 is connected with the import of sulfur dioxide crystallization tank 73 through pipeline; The outlet of sulfur dioxide crystallization tank 73 is connected with the import of ammonium sulfate product centrifuge 74 through pipeline, and the outlet of ammonium sulfate product centrifuge 74 is connected with the import of first mother liquor tank 75 through pipeline, and the outlet of first mother liquor tank 75 is connected with the 6th pump 77 through pipeline; The 6th pump 77 is connected with second spray equipment 714 through pipeline; Connect first pipeline 9 between the import of the 5th pump 76, 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 through pipeline, and 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 through blast pipe 7111; First cooling device 712, the cooling water inlet pipe of second cooling device 812 and the cooling water inlet pipe of first heat exchanger 3 link together, and first cooling device 712, the cooling water outlet pipe of second cooling device 812 and the cooling water outlet pipe of first heat exchanger 3 link together, and are 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 with the import of the 7th pump 86 through pipeline; The outlet of the 7th pump 86 is connected with the import of the 3rd heat exchanger 82 through pipeline, and the outlet siphunculus road of the 3rd heat exchanger 82 is connected with the import of carbon dioxide crystallization tank 83, and the outlet of carbon dioxide crystallization tank 83 is connected with the import of carbonic hydroammonium product centrifuge 84 through pipeline; The outlet of carbonic hydroammonium product centrifuge 84 is connected with the import of second mother liquor tank 85 through pipeline; The outlet of second mother liquor tank 85 is connected with the 8th pump 87 through pipeline, and the 8th pump 87 is connected with the 4th spray equipment 814 through 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 absorbing sulfur dioxide and carbon dioxide following:

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

(2) the coal-burning power plant's flue gas that will pass through after dedusting is handled with cooling gets into from the bottom on sulfur dioxide absorption tower 71; The weak aqua ammonia storage tank 11 interior weak aqua ammonia absorbent solutions that can capture absorbing sulfur dioxide spray downwards through first spray equipments 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 ℃ through first cooling device 712; Specifically be through 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 have absorbed sulfur dioxide and generated ammonium sulfate, and 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 through 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 through 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 through pipeline; And extract in second spray equipment 714 that pumps into sulfur dioxide absorption tower 71 spray downwards out through the 6th pump 77, the unsaturated ammonium sulfate of 71 bottoms, sulfur dioxide absorption tower through first pipeline 9, is directly pumped in second spray equipment 714 on sulfur dioxide absorption tower 71 spray downwards 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 through first pump 5 and in the sulfur dioxide absorption tower 71 of accomplishing after the ammonium sulfate fertilizer product separates, replenish high concentration ammoniacal liquor; Make the solution concentration in the sulfur dioxide absorption tower 71 return to the weak aqua ammonia absorbent solution concentration when 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 gets into 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 through 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 ℃ through second cooling device 812; Specifically be through 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 have absorbed carbon dioxide and have 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 through 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 through pipeline; And extract in the 4th spray equipment 814 that pumps into carbon dioxide absorption tower 81 spray downwards out through the 8th pump 87, the unsaturated carbonic acid hydrogen ammonium salt solution of carbon dioxide absorption tower 81 bottoms is through second pipeline 20, directly pumped in the 4th spray equipment 814 of carbon dioxide absorption tower 81 spray downwards 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 through second pump 6 and in the carbon dioxide absorption tower of accomplishing after the ammonium bicarbonate fertilizer product separates 81, replenish high concentration ammoniacal liquor; Make the solution concentration in the carbon dioxide absorption tower 81 return to the weak aqua ammonia absorbent solution concentration when beginning, promptly mass percent is between the 6%-8%;

(10) circulation above-mentioned steps.

Ammonia process normal pressure of the present invention captures absorbing sulfur dioxide and carbon dioxide system makes sulfur dioxide, carbon dioxide in coal-burning power plant's flue gas generate ammonium sulfate and ammonium bicarbonate soln respectively with the reverse full contact reaction of weak aqua ammonia absorbent solution respectively through adopting sulfur dioxide absorption tower 71 and carbon dioxide absorption tower 81; And apply in a flexible way unsaturated ammonium sulfate, the ammonium bicarbonate soln produced and increased benefit high strength ammonia water conservancy project preface and sulfur dioxide absorption tower 71, carbon dioxide absorption tower 81 in establish first cooling device 712 and second cooling device 812 respectively; The desired production status of ability this technology of better controlling; 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, the more effective capture absorbability that has improved coal-burning power plant's sulfur dioxide of flue gases, carbon dioxide of while, this technological process simplification, system architecture simplification, investment and operating cost are cheap.

The above embodiment describes preferred implementation of the present invention; Be not that scope of the present invention is limited; Design under the prerequisite of spirit not breaking away from the present invention; Various distortion and improvement that the common engineers and technicians in this area make technical scheme of the present invention all should fall in the definite protection domain of claims of the present invention.

Claims (2)

1. an ammonia process normal pressure captures absorbing 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 and second pump (5,6), apparatus for absorbing SO 2 (7) and absorption unit of dioxide carbon (8); Said apparatus for absorbing SO 2 (7) 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) and the 5th, six pumps (76,77) of normal pressure, and said sulfur dioxide absorption tower (71) comprises first cooling device (712) in first tank body (711), the tank body and first and second spray equipment (713 that tank body is interior upward, the middle part is provided with respectively; 714), said 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, eight pumps (86,87) of normal pressure; Said carbon dioxide absorption tower (81) comprise in second cooling device (812) and the tank body in second tank body (811), tank body go up, third and fourth spray equipment (813,814) that the middle part is provided with respectively, said weak aqua ammonia feedway (1) through pipeline respectively with said first and third spray equipment (713; 813) connect, said air-introduced machine (2) is connected with the air inlet of first heat exchanger (3) through pipeline, and the exhaust outlet of said first heat exchanger (3) stretches into said first tank body (711) inner chamber bottom through pipeline; Said first tank body (711) bottom is connected with the import of the 5th pump (76) through pipeline, and the outlet of said the 5th pump (76) is connected with the import of second heat exchanger (72) through pipeline, and the outlet of said second heat exchanger (72) is connected with the import of sulfur dioxide crystallization tank (73) through pipeline; The outlet of said sulfur dioxide crystallization tank (73) is connected with the import of ammonium sulfate product centrifuge (74) through pipeline, and the outlet of said ammonium sulfate product centrifuge (74) is connected with the import of first mother liquor tank (75) through pipeline, and the outlet of said first mother liquor tank (75) is connected with the 6th pump (77) through pipeline; Said the 6th pump (77) is connected with said second spray equipment (714) through pipeline, connects first pipeline (9) between the import of said the 5th, six pumps (76,77); Said high concentration ammoniacal liquor storage tank (4) connects said first and second pump (5 with the import of first and second pump (5,6) respectively through pipeline; 6) outlet respectively with second, four spray equipments (714; 814) connect, said first tank body (711) top is communicated with said first and second cooling device (712 through blast pipe (7111) with second tank body (811) inner chamber bottom; The cooling water inlet pipe of cooling water inlet pipe 812) and first heat exchanger (3) links together; The cooling water outlet pipe of cooling water outlet pipe of said first and second cooling device (712,812) and first heat exchanger (3) links together, and is respectively arranged with first and second control valve (10 on the said cooling water inlet pipe; 50); Said second tank body (811) bottom is connected with the import of the 7th pump (86) through pipeline, and the outlet of said the 7th pump (86) is connected with the import of the 3rd heat exchanger (82) through pipeline, and the outlet siphunculus road of said the 3rd heat exchanger (82) is connected with the import of carbon dioxide crystallization tank (83); The outlet of said carbon dioxide crystallization tank (83) is connected with the import of carbonic hydroammonium product centrifuge (84) through pipeline; The outlet of said carbonic hydroammonium product centrifuge (84) is connected with the import of second mother liquor tank (85) through pipeline, and the outlet of said second mother liquor tank (85) is connected with the 8th pump (87) through pipeline, and said the 8th pump (87) is connected with said the 4th spray equipment (814) through pipeline; Connect second pipeline (20) between the import of said the 7th, eight pumps (86,87).
2. ammonia process normal pressure as claimed in claim 1 captures absorbing sulfur dioxide and carbon dioxide system, it is characterized in that: said weak aqua ammonia feedway (1) is made up of weak aqua ammonia storage tank (11) and third and fourth pump (12,13); Said weak aqua ammonia storage tank (11) connects said third and fourth pump (12 with the import of third and fourth pump (12,13) respectively through pipeline; 13) outlet respectively with said first and third spray equipment (713; 813) connect, be respectively arranged with valve (30,40) on the said pipeline.
CN2011100393632A 2011-02-16 2011-02-16 System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method CN102120137B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2011100393632A CN102120137B (en) 2011-02-16 2011-02-16 System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
CN2011100393632A CN102120137B (en) 2011-02-16 2011-02-16 System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method
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

Publications (2)

Publication Number Publication Date
CN102120137A CN102120137A (en) 2011-07-13
CN102120137B true CN102120137B (en) 2012-12-26

Family

ID=44248857

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2011100393632A CN102120137B (en) 2011-02-16 2011-02-16 System and process for capturing and absorbing sulfur dioxide and carbon dioxide at normal pressure by using ammonia method

Country Status (1)

Country Link
CN (1) CN102120137B (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
CN102671531B (en) * 2012-05-18 2014-06-11 华北电力大学(保定) Method and device for absorbing fume pollutants by using ammonia water as absorbent
KR20160003878U (en) * 2015-04-30 2016-11-09 밍-시앙 양 Carbon dioxide gas treatment system
CN104923048A (en) * 2015-07-01 2015-09-23 碧水蓝天环保集团有限公司 Method for removing coal-fired flue gas pollutants and system for removing coal-fired flue gas pollutants
CN109529549A (en) * 2017-09-22 2019-03-29 江苏新世纪江南环保股份有限公司 Ultra-clean ammonia-process desulfurization technique is applied to the method for carbon capture process

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN201135851Y (en) * 2007-11-29 2008-10-22 武汉凯迪电力环保有限公司 A system for removing the carbon dioxide in flue gas of the generating plant using ammonia process
CN101422691B (en) * 2008-11-20 2011-12-07 武汉凯迪电力环保有限公司 Multi-pollutant removing technique and device of fuel coal smoke
CN202006081U (en) * 2011-02-16 2011-10-12 安徽淮化股份有限公司 System for trapping and absorbing sulfur dioxide and carbon dioxide at normal pressure through ammonia process

Also Published As

Publication number Publication date
CN102120137A (en) 2011-07-13

Similar Documents

Publication Publication Date Title
CN101579602B (en) Energy-saving and high-quality ammonia desulphurization process for ammonia sulfate recovery
US9370745B2 (en) Flue gas-treating method and apparatus for treating acidic tail gas by using ammonia process
CN201380037Y (en) Flue-gas cleaner with functions of desulphurization, denitration, concentration and crystal
CN103303877B (en) Many sources of the gas low concentration SO 2smoke comprehensive reclaims acid-making process flow process
KR20100116582A (en) Promoter enhanced chilled ammonia based system and method for removal of co2 from flue gas stream
CN105056749A (en) System and method for removing nitric oxides and sulfur oxides in flue gas simultaneously
CN103936036B (en) Integrated carbon dioxide removes and ammonia-soda process
CN100490946C (en) Sintering flue gas ammonia method desulfurizing system
CN103223292B (en) Ammonia process flue gas treatment method for acidic tail gas and device
CN101797470B (en) Method for circularly trapping SO2 and CO2 by using calcium-based absorbent
CN101524620B (en) Segment-based ammonia method flue gas desulfurization device
CN102000486B (en) Method for catching carbon dioxide in flue gas by active sodium carbonate and apparatus thereof
CN101343077B (en) Method for preparing gypsum by removing boiler flue gas sulphur dioxide with white slime from ammonia alkali factory
US8168148B2 (en) Flue-gas purification and reclamation system and method thereof
CN101745305A (en) Method for removing various gaseous pollutants from smoke gas
CN201320447Y (en) Integrated smoke purification device for desulphurization and denitration
CN100551494C (en) Ammonia process removes the method and the system thereof of carbon dioxide in the generating plant flue gas
CN100531867C (en) Method and apparatus for combined removing sulfur-dioxide and nitrogen oxide by mixed solution
CN104190220B (en) Coke oven flue gas denitrification apparatus and method
JP4959303B2 (en) Exhaust gas treatment method and treatment apparatus
CN201912884U (en) Ammonia desulfurizer with two-level gas distributors
JP6171096B2 (en) Semi-dry simultaneous desulfurization / denitration / demercury equipment and method using circulating fluidized bed
CN200998639Y (en) Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower
CN102179146B (en) Smoke desulfuration and denitration system absorbed by dielectric barrier discharge combined lye and process thereof
CN104826463B (en) A kind of sour gas produces NaHS technique and device

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant