CN113996171A - Industrial flue gas desulfurization, denitrification and decarburization system and treatment method - Google Patents

Industrial flue gas desulfurization, denitrification and decarburization system and treatment method Download PDF

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CN113996171A
CN113996171A CN202111310547.8A CN202111310547A CN113996171A CN 113996171 A CN113996171 A CN 113996171A CN 202111310547 A CN202111310547 A CN 202111310547A CN 113996171 A CN113996171 A CN 113996171A
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flue gas
solid
denitration
tank
treatment
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姜正雄
邓云天
安雷
叶紫青
韩志涛
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Sec Ihi Power Generation Environment Protection Engineering Co ltd
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Sec Ihi Power Generation Environment Protection Engineering Co ltd
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    • 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
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • 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
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen 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
    • B01D53/46—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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/10—Oxidants
    • B01D2251/108—Halogens or halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination

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Abstract

The invention provides an industrial flue gas desulfurization, denitrification and decarbonization system and a treatment method, and relates to the technical field of industrial flue gas treatmentThe physical unit comprises a flue gas desulfurization module, a flue gas denitration module and a flue gas decarburization module; the invention utilizes strong alkaline solution generated by seawater electrolysis to treat seawater desalination wastewater to obtain Mg (OH)2、Ca(OH)2Precipitating to recover metal ions, recovering Mg (OH)2、Ca(OH)2The treated waste liquid is used for desulfurizing and decarbonizing flue gas, and then CaSO is separated from the desulfurized and decarbonized waste liquid4、MgCO3、CaCO3The method can realize the desulfurization and decarburization of the flue gas, can realize the recovery of products and the reutilization of resources, achieves the aim of treating wastes with processes of wastes against one another, and saves the flue gas treatment cost.

Description

Industrial flue gas desulfurization, denitrification and decarburization system and treatment method
Technical Field
The invention belongs to the technical field of industrial flue gas treatment, and particularly relates to a desulfurization, denitrification and decarburization system and a treatment method for industrial flue gas.
Background
The seawater desalination is one of effective methods for preparing fresh water due to simple principle, easy realization and large fresh water yield, and the problem of shortage of fresh water resources in part of regions can be effectively solved through seawater desalination. However, the desalinated wastewater contains high-concentration salt, and if the desalinated wastewater is directly discharged without being treated, the desalinated wastewater can seriously affect the natural ecology. At present, a dilution method is generally adopted to dilute salt in the wastewater and then discharge the salt into the sea, so that resource waste is caused. The seawater desalination wastewater is treated and then recycled, which is an effective way for solving the problem of direct discharge of the desalination wastewater.
The industrial flue gas contains a large amount of SO2NOx and CO2The industrial flue gas is directly discharged without being treated, which causes serious pollution to the atmospheric environment, and the discharge of the industrial flue gas is strictly limited internationally and domestically. At present, dry and wet methods are generally adopted to carry out desulfurization treatment on flue gas, wherein the calcium-based wet desulfurization technology is widely applied due to the advantages of high desulfurization efficiency, simple and convenient equipment operation and maintenance, low cost and the like. At present, the mature flue gas denitration technology is mainly an SCR technology, but has the problems of large equipment investment, high operation cost, narrow reaction temperature window, easy poisoning and invalidation of a catalyst and the like; the wet method technology for removing the nitric oxide in the flue gas has great prospect, but the NO content in the industrial flue gas nitric oxide is up to more than 90 percent, the NO dissolubility is poor, and the nitric oxide is difficult to be directly removed by the wet method technology, so that oxygen is adoptedThe oxidation of NO to highly-valent and readily-soluble NOx by the chemical process followed by removal by wet process technology is an effective process. CO 22Is a greenhouse gas, and can be used for treating CO in flue gas2Absorbing to reduce CO2The emission has important significance for relieving the greenhouse effect, but at present, mature flue gas CO does not exist2And (4) removing technology.
In order to solve the problems of multiple required devices, complex process and high cost caused by independent desulfurization and denitration in the prior industrial flue gas treatment, the patent with the publication number of CN208406557U discloses an industrial flue gas treatment system, wherein a desulfurization reactor is connected with a denitration reactor, a desulfurizer and an ammonia inlet are arranged on the desulfurization reactor, and a flue gas dust remover is also arranged on the desulfurization reactor. However, in order to maintain the desulfurization effect, an additional desulfurizing agent is required, which increases the desulfurization cost; and the system can not effectively remove CO in the flue gas2。
Therefore, the system and the method for treating the industrial flue gas by using the seawater desalination wastewater are very important, and not only can change waste into valuable, but also can utilize the seawater desalination wastewater, treat the waste by using the waste and realize resource recovery.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a system and a treatment method for performing desulfurization, denitrification and decarburization on industrial flue gas by using seawater desalination wastewater, so as to solve the problems in the background art.
In order to achieve the purpose, the invention provides an industrial flue gas desulfurization, denitrification and decarbonization system which comprises a seawater electrolysis unit, a seawater desalination wastewater treatment unit and an industrial flue gas treatment unit which are sequentially connected, wherein the seawater desalination wastewater treatment unit comprises a metal ion separation module and a metal hydroxide treatment module, and the industrial flue gas treatment unit comprises a flue gas desulfurization module, a flue gas denitrification module and a flue gas decarbonization module.
Further, the seawater electrolysis unit comprises a diaphragm electrolysis cell and a hydrogen storage tank.
Further, the seawater desalination wastewater treatment unit comprises a metal ion separation module and a metal hydroxide treatment module;
the metal ion separation module comprises a primary sedimentation tank, a secondary sedimentation tank, a first solid-liquid separator, a second solid-liquid separator and Mg (OH)2Storage cabinet, Ca (OH)2A storage cabinet and an alkali liquor pool;
the liquid outlet of the cathode pool of the diaphragm electrolytic cell is respectively connected with the primary sedimentation tank and the secondary sedimentation tank, the primary sedimentation tank is connected with the first solid-liquid separator, the sedimentation outlet of the first solid-liquid separator is connected with the Mg (OH)2The storage cabinet is connected, the solution outlet of the first solid-liquid separator is connected with the secondary sedimentation tank, the secondary sedimentation tank is connected with the second solid-liquid separator, and the sedimentation outlet of the second solid-liquid separator is connected with Ca (OH)2The storage cabinet is connected, and a solution outlet of the second solid-liquid separation tank is connected with the alkali liquor tank;
the metal hydroxide treatment module comprises Mg (OH)2Treatment tank and Ca (OH)2Slurry pool of said Mg (OH)2The treatment tank is connected with the Mg (OH)2 storage cabinet, the Ca (OH)2Serous fluid pool with said Ca (OH)2The storage cabinets are connected.
Further, the flue gas desulfurization module comprises a flue gas desulfurization module, a flue gas denitration module and a flue gas decarburization module;
the flue gas desulfurization module comprises a desulfurization tower, a third solid-liquid separator and a CaSO which are connected in sequence4A storage cabinet, the desulfurizing tower and the Ca (OH)2Connecting the slurry pools;
the flue gas denitration module comprises a denitration tower and a denitration waste liquid treatment tank which are sequentially connected, the denitration tower is connected with a liquid outlet of an anode tank of the diaphragm electrolytic tank, and a smoke outlet of the denitration tower is connected with a smoke inlet of the denitration tower;
the flue gas decarbonization module comprises CO2An absorption tower, a first carbonate treatment pool, a second carbonate treatment pool, a fourth solid-liquid separator, a fifth solid-liquid separator and CaCO3Storage cabinet and MgCO3Storage cabinet；
The smoke outlet of the denitration tower and the CO2The smoke inlet of the absorption tower is connected; the CO is2The absorption tower is connected with the alkali liquor pool, and the CO is2A liquid outlet of the absorption tower is respectively connected with the first carbonate treatment pool and the second carbonate treatment pool, and the first carbonate treatment pool, the fourth solid-liquid separator and the CaCO3The storage cabinets are connected in sequence, and the second carbonate treatment pool, the fifth solid-liquid separator and the MgCO are3The storage cabinets are connected in sequence, and the first carbonate treatment pool is connected with the Ca (OH)2A storage cabinet connected to said second carbonate treatment tank and said Mg (OH)2The treatment pools are connected.
A treatment method for desulfurization, denitrification and decarburization of industrial flue gas comprises the following steps:
step S1: electrolyzing seawater;
step S2: separating metal ions in the seawater desalination wastewater;
step S3: treating the metal hydroxide;
step S4: desulfurizing flue gas;
step S5: denitration of flue gas;
step S6: and (4) decarbonizing the flue gas.
Further, the industrial flue gas desulfurization, denitrification and decarburization system is adopted; the specific process of step S1 is to electrolyze seawater by using a diaphragm electrolytic cell to generate a chlorine-containing solution with oxidability in an anode cell and a NaOH solution and hydrogen in a cathode cell, and store the hydrogen in a hydrogen storage tank;
the main reactions involved in the electrolysis of seawater using diaphragm cells are as follows:
anode: 2Cl-→Cl2+2e-
Cathode: 2H2O+2e-→2OH-+H2
Anode pool: cl2+OH-→ClO-+Cl-+H2O
ClO-+H2O→HClO+OH-
HClO→H++ClO-
The concrete process of the step S2 is that metal ions are separated by adopting a pH changing method, firstly NaOH solution generated by seawater electrolysis in the step S1 is added into a primary sedimentation tank, so that Mg in seawater desalination wastewater is enabled2+Completely precipitating, and separating Mg (OH) by using a first solid-liquid separator2Precipitation and solution separation, Mg (OH)2The precipitate is stored in Mg (OH)2In the storage cabinet, the separated solution is discharged into a secondary sedimentation tank; adding NaOH solution generated by electrolyzing seawater in step S1 into the secondary sedimentation tank to make Ca2+Completely precipitating, and separating Ca (OH) by using a second solid-liquid separator2Precipitation and solution separation, Ca (OH)2The precipitate is stored in Ca (OH)2And in the storage cabinet, discharging the separated solution into an alkaline solution pool.
The main reactions involved in the process of separating metal ions in seawater desalination wastewater are as follows:
Mg2++2OH-→Mg(OH)2
Ca2++2OH-→Ca(OH)2
further, the concrete procedure of step S3 is to process the metal hydroxide to obtain Mg (OH) through step S22The precipitate is discharged into Mg (OH)2In the treatment tank, to Mg (OH)2Adding hydrochloric acid into the treatment pool to Mg (OH)2Acidifying to obtain MgCl2A solution; a portion of Ca (OH) obtained in step S22The precipitate is discharged into Ca (OH)2And preparing slurry in the slurry pool.
The main reactions involved in the treatment of metal hydroxides are as follows:
Mg(OH)2+2H+→Mg2++2H2O
further, the specific process of step S4 is to desulfurize the flue gas by adding Ca (OH) obtained in step S32Spraying the slurry into the desulfurizing tower from the top of the desulfurizing tower, introducing industrial flue gas into the desulfurizing tower from a flue gas inlet at the bottom of the desulfurizing tower to desulfurize the industrial flue gas, and separating CaSO from the desulfurized waste liquid through a third solid-liquid separator4Precipitating and storing in CaSO4In the storage cabinet.
The main reactions involved in the flue gas desulfurization process are as follows:
SO2+H2O→SO3 2-+2H+
SO3 2-+O2+2H+→SO4 2-+H2O
Ca(OH)2+SO4 2-+2H+→CaSO4+2H2O
further, in the step S5, specifically, in the denitration of the flue gas, the chlorine-containing solution generated by electrolyzing the seawater in the step S1 is sprayed into the denitration tower from the top of the denitration tower, the flue gas desulfurized in the step S4 is introduced into the denitration tower from the flue gas inlet at the bottom of the denitration tower, the industrial flue gas is denitrated, and the denitration waste liquid is discharged into the denitration waste liquid treatment tank for treatment and then discharged.
The main reactions involved in the flue gas denitration process are as follows:
NO+ClO-→NO2+Cl-
NO+NO2+H2O→2H++2NO2 -
2NO2+H2O→2H++NO3-+NO2 -
2NO2+ClO-+H2O→2NO3 -+Cl-+2H+
NO2 -+ClO-→NO3 -+Cl-
3NO2+H2O→2H++2NO3 -+NO
further, the specific process of step S6 is to decarbonize the flue gas and remove CO from the alkali solution in the alkali solution pool of step S22Spraying CO into the top of the absorption tower2In the absorption tower, the flue gas denitrated in the step S5 is treated by CO2Introducing CO into a smoke inlet at the bottom of the absorption tower2In the absorption tower, the industrial flue gas is decarbonized, the decarbonized flue gas is directly discharged, the decarbonized waste liquid is discharged into a first carbonate treatment tank and a second carbonate treatment tank, and MgCl obtained in the step S3 is used2Adding the solution into a second carbonate treatment pool, and separating by a fifth solid-liquid separator to obtain MgCO3Precipitating and storing the precipitate in MgCO3A storage cabinet for storing part of Ca (OH) obtained in step S22Adding the precipitate into a first carbonate treatment tank, and separating by a fourth solid-liquid separator to obtain CaCO3The precipitate is stored in CaCO3And (7) storing the cabinet.
The main reactions involved in the process of flue gas decarburization are as follows:
CO2+2OH-→CO3 2-+H2O
Mg2++CO3 2-→MgCO3
Ca(OH)2+CO3 2-→CaCO3+2OH-
has the advantages that:
(1) the invention provides an industrial flue gas desulfurization, denitrification and decarbonization system which comprises a seawater electrolysis unit, a seawater desalination wastewater treatment unit and an industrial flue gas treatment unit which are sequentially connected, wherein the seawater desalination wastewater treatment unit comprises a metal ion separation module and a metal hydroxide treatment module, the industrial flue gas treatment unit comprises a flue gas desulfurization module, a flue gas denitrification module and a flue gas decarbonization module, hydrogen generated by seawater electrolysis through the seawater electrolysis unit can be collected and utilized, and high-salinity wastewater is treated through the seawater desalination wastewater treatment unit to obtain the metal hydroxide for flue gas desulfurization and decarbonization, so that the purpose of treating waste with waste is achieved, resources are recycled, and a desulfurizer, a denitrifier and CO are not needed2The extra use of the absorbent saves the cost; has better effect of removing sulfur oxide, nitrogen oxide and carbon dioxide, and realizes the secondary recovery of products from the waste liquid of the flue gas treatment.
(2) The invention provides a treatment method for desulfurization, denitrification and decarburization of industrial flue gas, which is characterized in that strong alkaline solution generated by seawater electrolysis is utilized to treat seawater desalination wastewater to obtain Mg (OH)2、Ca(OH)2Precipitation can realize the recovery of metal ions; recovering Mg (OH)2、Ca(OH)2After treatment, the obtained product is used for desulfurization and decarbonization of flue gas, and then is separated from desulfurization and decarbonization waste liquorCaSO4、MgCO3、CaCO3The method can realize the desulfurization and decarburization of the flue gas, and can realize the recovery of products and the reutilization of resources. Meanwhile, the strong oxidizing solution generated by electrolyzing seawater can be used for flue gas denitration; by the method, the problems of seawater desalination wastewater discharge and industrial flue gas treatment are solved, resources are recycled, the purpose of treating wastes with processes of wastes against one another is achieved, the flue gas treatment cost is saved, the resources are recycled, and the method has important practical significance.
The conception, the specific structure and the technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, the features and the effects of the present invention.
Drawings
FIG. 1 is a schematic structural diagram of a preferred embodiment of the present invention;
description of the drawings:
1. a diaphragm electrolytic cell; 2. a hydrogen storage tank; 3. a first-stage sedimentation tank; 4. a first solid-liquid separator; 5. a secondary sedimentation tank; 6. mg (OH)2A storage cabinet; 7. a second solid-liquid separator; 8. an alkaline solution pool; 9. mg (OH)2A treatment tank; 10. ca (OH)2A storage cabinet; 11. ca (OH)2A slurry tank; 12. a desulfurizing tower; 13. a denitration tower; 14. CO 22An absorption tower; 15. a third solid-liquid separator; 16. a denitration waste liquid treatment tank; 17. a first carbonate treatment tank; 18. a second carbonate treatment tank; 19. CaSO4A storage cabinet; 20. a fourth solid-liquid separator; 21. a fifth solid-liquid separator; 22. CaCO3A storage cabinet; 23. MgCO3And (7) storing the cabinet.
Detailed Description
The invention will be further illustrated with reference to specific embodiments. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and such equivalents may fall within the scope of the present invention as defined in the appended claims.
In the drawings, structurally identical elements are represented by like reference numerals, and structurally or functionally similar elements are represented by like reference numerals throughout the several views. The size and thickness of each component shown in the drawings are arbitrarily illustrated, and the present invention is not limited to the size and thickness of each component. The thickness of the components may be exaggerated where appropriate in the figures to improve clarity.
Example (b):
as shown in fig. 1, in a preferred embodiment, the present invention provides an industrial flue gas desulfurization, denitrification and decarbonization system, which comprises a seawater electrolysis unit, a seawater desalination wastewater treatment unit and an industrial flue gas treatment unit, which are connected in sequence, wherein the seawater desalination wastewater treatment unit comprises a metal ion separation module and a metal hydroxide treatment module, and the industrial flue gas treatment unit comprises a flue gas desulfurization module, a flue gas denitrification module and a flue gas decarbonization module.
The seawater electrolysis unit comprises a diaphragm electrolysis cell 1 and a hydrogen storage tank 2;
the metal ion separation module comprises a primary sedimentation tank 3, a secondary sedimentation tank 5, a first solid-liquid separator 4, a second solid-liquid separator 7, Mg (OH)2 Storage cabinet 6, Ca (OH)2A storage cabinet 10 and an alkali liquor pool 8;
the liquid outlet of the cathode pool of the diaphragm electrolytic cell 1 is respectively connected with a primary sedimentation tank 3 and a secondary sedimentation tank 5, the primary sedimentation tank 3 is connected with a first solid-liquid separator 4, the sedimentation outlet of the first solid-liquid separator 4 is connected with Mg (OH)2The storage cabinet 6 is connected, the solution outlet of the first solid-liquid separator 4 is connected with the secondary sedimentation tank 5, the secondary sedimentation tank 5 is connected with the second solid-liquid separator 7, the sedimentation outlet of the second solid-liquid separator 7 is connected with Ca (OH)2The storage cabinet 10 is connected, and the solution outlet of the second solid-liquid separation tank is connected with the alkali liquor tank 8.
The metal hydroxide treatment module comprises Mg (OH)2Treatment tank 9 and Ca (OH)2 Slurry pool 11, Mg (OH)2Treatment tank 9 with Mg (OH)2 Storage cabinet 6 connection, Ca (OH)2 Slurry pool 11 with Ca (OH)2The storage cabinets 10 are connected.
The flue gas desulfurization module comprises a desulfurization tower 12, a third solid-liquid separator 15 and a CaSO which are connected in sequence4Storage cabinet 19, desulfurizing tower 12 and Ca (OH)2The slurry pool 11 is connected withAnd (6) connecting.
The flue gas denitration module is including the denitration tower 13 and the denitration waste liquid treatment pond 16 that connect gradually, and denitration tower 13 is connected with the positive pole pond liquid outlet of diaphragm electrolytic cell 1, and the exhaust port of desulfurizing tower 12 is connected with the inlet flue gas mouth of denitration tower 13.
The flue gas decarbonization module comprises CO2 An absorption tower 14, a first carbonate treatment tank 17, a second carbonate treatment tank 18, a fourth solid-liquid separator 20, a fifth solid-liquid separator 21, CaCO3Storage cabinet 22 and MgCO3 A storage cabinet 23;
flue outlet and CO of denitration tower 132The smoke inlet of the absorption tower 14 is connected; CO 22The absorption tower 14 is connected with the alkali liquor pool 8, CO2The liquid outlet of the absorption tower 14 is respectively connected with a first carbonate treatment tank 17, a second carbonate treatment tank 18, the first carbonate treatment tank 17, a fourth solid-liquid separator 20 and CaCO3The storage cabinet 22 is connected in sequence with the second carbonate treatment tank 18, the fifth solid-liquid separator 21 and the MgCO3The storage cabinet 23 is connected in sequence, the first carbonate treatment pool 17 and Ca (OH)2A storage cabinet 10 connected with a second carbonate treatment tank 18 and Mg (OH)2The treatment tanks 9 are connected.
The method for treating the industrial flue gas by using the industrial flue gas desulfurization, denitrification and decarbonization system comprises the following steps:
step S1: electrolyzing seawater by using a diaphragm electrolytic cell 1, generating a chlorine-containing solution with oxidability in an anode cell, generating a NaOH solution and hydrogen in a cathode cell, and storing the hydrogen in a hydrogen storage tank 2;
step S2: : separating metal ions by adopting a pH changing method, firstly adding NaOH solution generated by seawater electrolysis in the step S1 into the primary sedimentation tank 3, and adjusting the pH to ensure that Mg in the seawater desalination wastewater2+Completely precipitating, and adding Mg (OH) by using a first solid-liquid separator 42Precipitation and solution separation, Mg (OH)2The precipitate is stored in Mg (OH)2In the storage cabinet 6, the separated solution is discharged into a secondary sedimentation tank 5; then adding NaOH solution generated by electrolyzing seawater in step S1 into the secondary sedimentation tank 5 to adjust pH so that Ca is generated2+Completely precipitating, and adding Ca (OH) into the solution by using a second solid-liquid separator 72Precipitation and solution separation, Ca (OH)2The precipitate is stored in Ca (OH)2In the tank 10, the separated solution is discharged to the lye tank 8.
Step S3: the Mg (OH) obtained in step S22The precipitate is discharged into Mg (OH)2In the treatment tank 9, the water is treated with Mg (OH)2Adding hydrochloric acid p-Mg (OH) into a treatment pool 92Acidifying to obtain MgCl2A solution; a portion of Ca (OH) obtained in step S22The precipitate is discharged into Ca (OH)2Slurry is made in the slurry tank 11.
Step S4: the Ca (OH) obtained in step S32The slurry is sprayed into the desulfurizing tower 12 from the top of the desulfurizing tower 12 through a slurry pump, the desulfurizing tower 12 is a spray tower, industrial flue gas is introduced into the desulfurizing tower 12 from a flue gas inlet at the bottom of the desulfurizing tower 12 to be desulfurized, the desulfurization efficiency is improved through gas-liquid countercurrent contact, and CaSO is separated from the desulfurized waste liquid through a third solid-liquid separator 154Precipitating and storing in CaSO4In the storage cabinet 19, the separated waste liquid is directly discharged.
Step S5: and (3) spraying the chlorine-containing solution generated by electrolyzing the seawater in the step S1 into the denitration tower 13 from the top of the denitration tower 13 through a spray pump, wherein the denitration tower 13 is a spray tower, the flue gas desulfurized in the step S4 is introduced into the denitration tower 13 from a flue gas inlet at the bottom of the denitration tower 13, the industrial flue gas is denitrated, the denitration efficiency is improved through gas-liquid countercurrent contact, and the denitration waste liquid is discharged into the denitration waste liquid treatment tank 16 for treatment and then discharged.
Step S6: the alkali liquor in the alkali liquor pool 8 of the step S2 is sprayed from CO through a spray pump2CO is injected into the top of the absorption column 142In the absorption tower 14, the flue gas denitrated in step S5 is CO-derived2CO is introduced into a smoke inlet at the bottom of the absorption tower 142In the absorption tower 14, CO2The absorption tower 14 is a spray tower for decarbonizing the industrial flue gas and increasing CO by gas-liquid countercurrent contact2Absorption efficiency, direct emission of decarbonized flue gas, discharge of decarbonized waste liquid into the first carbonate treatment tank 17 and the second carbonate treatment tank 18, and MgCl obtained in step S32The solution is added into a second carbonate treatment pool 18 and separated by a fifth solid-liquid separator 21 to obtain MgCO3Precipitating and storing the precipitate in MgCO3 A storage cabinet 23 for storing the product obtained in step S2Part of Ca (OH)2The precipitate is added into the first carbonate treatment tank 17 and separated by the fourth solid-liquid separator 20 to obtain CaCO3The precipitate is stored in CaCO3And the storage cabinet 22 directly discharges the waste liquid after being separated by the fourth solid-liquid separator 20 and the fifth solid-liquid separator 21.

Claims (10)

1. The utility model provides an industrial flue gas desulfurization denitration decarbonization system which characterized in that, including the sea water electrolysis unit, sea water desalination wastewater treatment unit and the industrial flue gas processing unit that connect gradually, sea water desalination wastewater treatment unit includes metal ion separation module and metal hydroxide processing module, industrial flue gas processing unit includes flue gas desulfurization module, flue gas denitration module and flue gas decarbonization module.
2. The system for desulfurization, denitrification and decarburization of industrial flue gas according to claim 1, wherein the seawater electrolysis unit comprises a diaphragm electrolysis cell (1) and a hydrogen storage tank (2);
the metal ion separation module comprises a primary sedimentation tank (3), a secondary sedimentation tank (5), a first solid-liquid separator (4), a second solid-liquid separator (7), Mg (OH)2Storage cabinet (6), Ca (OH)2A storage cabinet (10) and an alkali liquor pool (8);
the liquid outlet of the cathode pool of the diaphragm electrolytic cell (1) is respectively connected with the primary sedimentation tank (3) and the secondary sedimentation tank (5), the primary sedimentation tank (3) is connected with the first solid-liquid separator (4), the sedimentation outlet of the first solid-liquid separator (4) is connected with the Mg (OH)2A storage cabinet (6) is connected, a solution outlet of the first solid-liquid separator (4) is connected with the secondary sedimentation tank (5), the secondary sedimentation tank (5) is connected with the second solid-liquid separator (7), and a sedimentation outlet of the second solid-liquid separator (7) is connected with Ca (OH)2The storage cabinet (10) is connected, and the solution outlet of the second solid-liquid separation tank is connected with the alkali liquor tank (8).
3. The system of claim 2, wherein the metal hydroxide treatment module comprises Mg (OH)2A treatment tank (9) and Ca: (OH)2A slurry pool (11), said Mg (OH)2Treatment basin (9) with the Mg (OH)2A storage cabinet (6) is connected, the Ca (OH)2Serous fluid pool with said Ca (OH)2The storage cabinets (10) are connected.
4. The system of claim 3, wherein the flue gas desulfurization module comprises a desulfurization tower (12), a third solid-liquid separator (15) and a CaSO connected in sequence4A storage cabinet (19), the desulfurizing tower (12) and the Ca (OH)2The slurry pool (11) is connected;
the flue gas denitration module comprises a denitration tower (13) and a denitration waste liquid treatment tank (16) which are sequentially connected, wherein an anode tank liquid outlet of the diaphragm electrolytic tank (1) is connected with the denitration tower (13), and a smoke outlet of the denitration tower (12) is connected with a smoke inlet of the denitration tower (13);
the flue gas decarbonization module comprises CO2An absorption tower (14), a first carbonate treatment pool (17), a second carbonate treatment pool (18), a fourth solid-liquid separator (20), a fifth solid-liquid separator (21), CaCO3A storage cabinet (22) and MgCO3A cabinet (23);
the smoke outlet of the denitration tower (13) and the CO2The smoke inlet of the absorption tower (14) is connected; the CO is2An absorption tower (14) is connected with the alkali liquor pool (8), and the CO is2A liquid outlet of the absorption tower (14) is respectively connected with the first carbonate treatment pool (17) and the second carbonate treatment pool (18), and the first carbonate treatment pool (17), the fourth solid-liquid separator (20) and the CaCO3The storage cabinets (22) are connected in sequence, and the second carbonate treatment pool (18), the fifth solid-liquid separator (21) and the MgCO are3The storage cabinets (23) are sequentially connected, and the first carbonate treatment pool (17) is connected with the Ca (OH)2A storage cabinet (10) connected to said second carbonate treatment tank (18) and said Mg (OH)2The treatment pools (9) are connected.
5. A treatment method for desulfurization, denitrification and decarburization of industrial flue gas is characterized by comprising the following steps:
step S1: electrolyzing seawater;
step S2: separating metal ions in the seawater desalination wastewater;
step S3: treating the metal hydroxide;
step S4: desulfurizing flue gas;
step S5: denitration of flue gas;
step S6: and (4) decarbonizing the flue gas.
6. The method for desulfurization, denitrification and decarburization treatment of industrial flue gas according to claim 5, wherein the desulfurization, denitrification and decarburization system of industrial flue gas according to claim 4 is adopted; the specific process of the step S1 is that seawater is electrolyzed by a diaphragm electrolytic cell (1), a chlorine solution with oxidability is generated in an anode cell, a NaOH solution and hydrogen are generated in a cathode cell, and the hydrogen is stored in a hydrogen storage tank (2);
the concrete process of the step S2 is that metal ions are separated by adopting a pH changing method, firstly NaOH solution generated by seawater electrolysis in the step S1 is added into a primary sedimentation tank (3) to ensure that Mg in seawater desalination wastewater2+Completely precipitating, and adding Mg (OH) by a first solid-liquid separator (4)2Precipitation and solution separation, Mg (OH)2The precipitate is stored in Mg (OH)2In the storage cabinet (6), the separated solution is discharged into a secondary sedimentation tank (5); adding NaOH solution generated by electrolyzing seawater in step S1 into the secondary sedimentation tank (5) to make Ca2+Completely precipitating, and adding Ca (OH) by using a second solid-liquid separator (7)2Precipitation and solution separation, Ca (OH)2The precipitate is stored in Ca (OH)2In the storage cabinet (10), the separated solution is discharged into an alkaline solution pool (8).
7. The method of claim 6, wherein the step S3 comprises treating metal hydroxide to obtain Mg (OH) through step S22The precipitate is discharged into Mg (OH)2In the treatment tank (9), the water is treated with Mg (OH)2Adding hydrochloric acid to Mg (OH) in a treatment pool (9)2Acidifying to obtain MgCl2A solution; a portion of Ca (OH) obtained in step S22The precipitate is discharged into Ca (OH)2And preparing slurry in the slurry pool (11).
8. The method of claim 7, wherein the step S4 is a desulfurization step, in which Ca (OH) obtained in step S3 is added to the flue gas2The slurry is sprayed into the desulfurizing tower (12) from the top of the desulfurizing tower (12), the industrial flue gas is introduced into the desulfurizing tower (12) from a flue gas inlet at the bottom of the desulfurizing tower (12) to carry out desulfurization on the industrial flue gas, and CaSO is separated from the desulfurization waste liquid through a third solid-liquid separator (15)4Precipitating and storing in CaSO4In the storage cabinet (19).
9. The method of claim 7, wherein the step S5 includes denitration of flue gas, spraying chlorine-containing solution generated by electrolyzing seawater in the step S1 into the denitration tower (13) from the top of the denitration tower (13), introducing flue gas desulfurized in the step S4 into the denitration tower (13) from the flue gas inlet at the bottom of the denitration tower (13), denitration of the flue gas, and discharging the waste denitration liquid into the waste denitration liquid treatment tank (16).
10. The method of claim 7, wherein the step S6 is a flue gas decarburization process, in which the alkali solution in the alkali solution tank (8) of step S2 is extracted from CO2CO is sprayed into the top of the absorption tower (14)2In the absorption tower (14), the flue gas denitrated in the step S5 is treated by CO2CO is introduced into a smoke inlet at the bottom of the absorption tower (14)2In the absorption tower (14), the industrial flue gas is decarbonized, the decarbonized flue gas is directly discharged, the decarbonized waste liquid is discharged into a first carbonate treatment tank (17) and a second carbonate treatment tank (18), and MgCl obtained in the step S3 is used2The solution is added into a second carbonate treatment pool (18) and separated by a fifth solid-liquid separator (21) to obtain MgCO3Precipitating and storing the precipitate in MgCO3A storage cabinet (23), part of Ca (OH)2 precipitate obtained in the step S2 is added into the first carbonate treatment pool (17), and CaCO is obtained by separating through a fourth solid-liquid separator (20)3The precipitate is stored in CaCO3A storage cabinet (22).
CN202111310547.8A 2021-11-05 2021-11-05 Industrial flue gas desulfurization, denitrification and decarburization system and treatment method Pending CN113996171A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115138145A (en) * 2022-06-10 2022-10-04 上海市政工程设计研究总院（集团）有限公司 Carbon emission reduction method for sludge incineration

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115138145A (en) * 2022-06-10 2022-10-04 上海市政工程设计研究总院（集团）有限公司 Carbon emission reduction method for sludge incineration

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