CN110314500B - Wet deacidification equipment and method - Google Patents
Wet deacidification equipment and method Download PDFInfo
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- CN110314500B CN110314500B CN201910544257.6A CN201910544257A CN110314500B CN 110314500 B CN110314500 B CN 110314500B CN 201910544257 A CN201910544257 A CN 201910544257A CN 110314500 B CN110314500 B CN 110314500B
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- 238000000034 method Methods 0.000 title claims abstract description 45
- 238000005406 washing Methods 0.000 claims abstract description 141
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 63
- 239000003546 flue gas Substances 0.000 claims abstract description 63
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000002699 waste material Substances 0.000 claims abstract description 47
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 40
- 239000002253 acid Substances 0.000 claims abstract description 37
- 238000001556 precipitation Methods 0.000 claims abstract description 32
- 239000010865 sewage Substances 0.000 claims abstract description 32
- 150000003839 salts Chemical class 0.000 claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 20
- 239000007787 solid Substances 0.000 claims abstract description 12
- 239000000428 dust Substances 0.000 claims abstract description 10
- 238000000746 purification Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 68
- 239000002910 solid waste Substances 0.000 claims description 28
- 238000004062 sedimentation Methods 0.000 claims description 25
- 239000003513 alkali Substances 0.000 claims description 13
- 239000008235 industrial water Substances 0.000 claims description 13
- 230000018044 dehydration Effects 0.000 claims description 12
- 238000006297 dehydration reaction Methods 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 5
- -1 polytetrafluoroethylene Polymers 0.000 claims description 5
- 239000013589 supplement Substances 0.000 claims description 5
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- 229910001200 Ferrotitanium Inorganic materials 0.000 claims description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000011152 fibreglass Substances 0.000 claims description 3
- 239000010936 titanium Substances 0.000 claims description 3
- 238000005119 centrifugation Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 239000002351 wastewater Substances 0.000 description 14
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 12
- 231100001261 hazardous Toxicity 0.000 description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 239000011780 sodium chloride Substances 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000003518 caustics Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 230000002378 acidificating effect Effects 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000004891 communication Methods 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—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 by absorption
- B01D53/1418—Recovery of products
-
- 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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
-
- 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
- B01D53/14—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 by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/14—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 by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2045—Hydrochloric acid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- 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
- B01D2258/0291—Flue gases from waste incineration plants
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a wet deacidification device and a wet deacidification method, which are used in an incineration flue gas purification process, wherein the device comprises a first washing tower and a second washing tower which are communicated through a pipeline, the flue gas after dust removal passes through the first washing tower and then enters the second washing tower, the first washing tower comprises circulating water, the second washing tower comprises circulating saturated Na 2CO3 solution, the first washing tower is connected with a sewage treatment device or a waste materialization treatment production device, the circulating water in the first washing tower absorbs HCl in the flue gas and then generates hydrochloric acid, the hydrochloric acid flows to the sewage treatment device or the waste materialization treatment production device so as to be used for adjusting the pH value of the solution in the sewage treatment device or the waste materialization treatment production device, the bottom of the second washing tower is connected with a precipitation centrifugal separation device, the saturated Na 2CO3 solution reacts with acid gas in the flue gas to generate salt, and the precipitation centrifugal separation device separates the salt in a solid state.
Description
Technical Field
The invention relates to the field of flue gas purification treatment, in particular to efficient and economical wet deacidification equipment and method.
Background
In recent years, along with the rapid development of the environmental protection industry, a plurality of enterprises are actively entering the field of hazardous solid waste disposal, the hazardous solid waste in China is mainly disposed by adopting the incineration technology, along with the stricter national supervision on the environment, the standard discharge of flue gas in the incineration process is extremely important, generally, the contents of Cl and S elements in hazardous solid waste raw materials are higher, a large amount of HCl, SO 2 and other acidic gases in the flue gas are generated in the incineration process, and the wet deacidification has high removal efficiency on the HCl, SO 2 and other acidic gases in the flue gas, but the conventional wet deacidification process cannot avoid the treatment of a large amount of salt-containing wastewater, and the treatment cost and equipment investment of the part of salt-containing wastewater occupy a large proportion on the hazardous solid waste operation and equipment investment, SO that the operation cost of hazardous solid waste disposal can be greatly reduced and the equipment investment can be reduced to a certain extent if the generation of the salt-containing wastewater can be avoided in the wet deacidification process.
Accordingly, there is a need to propose an apparatus and a method for wet deacidification of incineration flue gas to at least partially solve the above-mentioned problems.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides wet deacidification equipment which is used in an incineration flue gas purification process and is characterized by comprising a first washing tower and a second washing tower which are communicated through a pipeline, wherein the flue gas after dust removal passes through the first washing tower and then enters the second washing tower,
Wherein the first washing tower comprises circulating water, the second washing tower comprises circulating saturated Na 2CO3 solution,
The first washing tower is connected with sewage treatment equipment or waste materialization treatment production equipment, the circulating water in the first washing tower absorbs HCl in the flue gas to generate hydrochloric acid, the hydrochloric acid flows to the sewage treatment equipment or the waste materialization treatment production equipment to be used for adjusting the pH value of the solution in the sewage treatment equipment or the waste materialization treatment production equipment,
The bottom of the second washing tower is connected with a precipitation centrifugal separation device, the saturated Na 2CO3 solution reacts with acid gas in the flue gas to generate salt, and the precipitation centrifugal separation device separates the salt in a solid state.
In one example, the first filter, the first circulating pump and the second circulating pump are arranged outside the first washing tower,
One end of the first filter is communicated with the interior of the first washing tower, the other end of the first filter is communicated with the first circulating pump, the first circulating pump is communicated with the interior of the first washing tower, the solution in the first washing tower passes through the first filter and is pumped into the first washing tower through the first circulating pump,
One end of the second circulating pump is communicated with the interior of the first washing tower, and the other end of the second circulating pump is connected with the industrial water supply device so as to supplement industrial water into the first washing tower.
In one example, the device also comprises a second filter, a third circulating pump, a fourth circulating pump and a saturated Na 2CO3 solution supply device which are arranged outside the second washing tower,
One end of the second filter is communicated with the interior of the second washing tower, the other end of the second filter is communicated with the third circulating pump, the third circulating pump is communicated with the interior of the first washing tower, the solution in the second washing tower passes through the second filter and is pumped into the first washing tower through the third circulating pump,
One end of the fourth circulating pump is communicated with the interior of the second washing tower, the other end of the fourth circulating pump is connected with the precipitation centrifugal separation device,
The saturated Na 2CO3 solution supply is in line communication with the second scrubber to provide a saturated Na 2CO3 solution to the second scrubber.
In one example, the sedimentation centrifugal separation device comprises a sedimentation device and a centrifugal device,
The sedimentation device is connected with the bottom of the second washing tower, the centrifugal device is connected with the sedimentation device, waste at the bottom of the second washing tower is discharged to the sedimentation device, and solid waste obtained after sedimentation is moved to the centrifugal device and is centrifugally dehydrated by the centrifugal device to obtain solid salt.
In one example, the sedimentation centrifugal separation device further comprises a secondary liquid device,
One end of the secondary liquid device is respectively connected with the sedimentation device and the centrifugal device, the other end of the secondary liquid device is connected with the fourth circulating pump, and liquid obtained after the waste is sedimented in the sedimentation device and liquid obtained after centrifugal dehydration of the centrifugal device enter the secondary liquid device and are pumped into the second washing tower through the fourth circulating pump.
In one example, the precipitation device comprises a precipitation tank and/or the centrifugal device comprises a centrifuge and/or the secondary liquid device comprises a circulating alkali liquid tank, the precipitation tank is made of titanium or carbon steel lined ceramic and/or the circulating alkali liquid tank is made of high-temperature glass fiber reinforced plastic.
In one example, the second filter comprises a basket filter.
In one example, the material of the liner of the basket filter comprises polytetrafluoroethylene.
In one example, an acid solution storage tank disposed between the first scrubber and the sewage treatment plant or waste disposal production plant is also included.
The invention also discloses a wet deacidification method which is used in the incineration flue gas purification process and is characterized in that the method adopts the equipment of any one of the above steps, and the method comprises the following steps:
1) Introducing the flue gas after dust removal into a first washing tower, discharging part of circulating water in the first washing tower to an acid solution storage tank when the pH value of circulating liquid in the first washing tower is lower than 3, and simultaneously opening a second circulating pump outside the first washing tower to supplement industrial water into the first washing tower;
2) Pumping saturated Na 2CO3 solution into the second washing tower through a third circulating pump outside the second washing tower, and absorbing acid gas in the flue gas entering the second washing tower after exiting from the first washing tower by using saturated Na 2CO3 solution; and
3) And discharging the waste in the second washing tower to a precipitation device in a continuous pollution discharge mode, wherein the solid waste and liquid obtained after the waste is precipitated by the precipitation device enter a centrifugal device for centrifugal dehydration, and the liquid obtained after the centrifugal dehydration and the liquid obtained after the precipitation are returned to the second washing tower together.
The invention provides novel equipment and a method for carrying out wet deacidification on incineration flue gas, the equipment comprises a first washing tower and a second washing tower which are communicated through a pipeline, the flue gas after dust removal passes through the first washing tower and then enters the second washing tower, wherein the first washing tower comprises circulating water, the second washing tower comprises circulating saturated Na 2CO3 solution, the first washing tower is connected with sewage treatment equipment or waste materialization treatment production equipment, the circulating water in the first washing tower absorbs HCl in the flue gas and then generates hydrochloric acid, the hydrochloric acid flows to the sewage treatment equipment or waste materialization treatment production equipment so as to be used for adjusting the pH value of the solution in the sewage treatment equipment or waste materialization treatment production equipment, the second washing tower is connected with a precipitation centrifugal separation device, and the precipitation centrifugal separation device separates salt generated by the reaction of saturated Na 2CO3 solution and acid gas in the flue gas in a solid state, and liquid obtained after precipitation and centrifugal dehydration is returned to the second washing tower.
The invention provides a high-efficiency and economical wet deacidification device and a method, wherein the wet deacidification method is characterized in that on one hand, hydrochloric acid is prepared from absorbed HCl in a first-stage washing tower and is used for a sewage treatment system to adjust pH; on the other hand, saturated Na 2CO3 solution is adopted in the secondary washing tower to further remove HCl and SO 2 in the flue gas, and simultaneously, solid waste salt is obtained in a mode of separating out NaCl and Na 2SO3 by controlling conditions in the process, SO that the generation of high-salt wastewater is avoided.
Compared with the prior art, the invention has the following advantages:
1. The invention prepares the hydrochloric acid by absorbing HCl in the flue gas, is used for adjusting the pH value of a sewage treatment system and a physical and chemical treatment production line, changes waste into valuable and reduces the operation cost.
2. The solid waste salt is obtained by adopting the way of separating out NaCl and Na 2SO3, so that the generation of high-salt-content waste water in the traditional wet deacidification process is avoided.
3. The invention adopts saturated Na 2CO3 solution to further absorb acid gas, and compared with the traditional method adopting NaOH solution for absorption, the cost of Na 2CO3 raw material is lower and more economic.
Drawings
The following drawings are included to provide an understanding of the invention and are incorporated in and constitute a part of this specification. The drawings illustrate embodiments of the invention and their description to explain the principles of the invention.
In the accompanying drawings:
Fig. 1 is a schematic structural view of an apparatus for wet deacidifying incineration flue gas in an embodiment of the present invention; and
Fig. 2 is a schematic flow diagram of a method for wet deacidifying incineration flue gas in one embodiment of the present invention.
Detailed Description
In the following description, numerous specific details are set forth in order to provide a more thorough understanding of the present invention. It will be apparent, however, to one skilled in the art that the invention may be practiced without one or more of these details. In other instances, well-known features have not been described in detail in order to avoid obscuring the invention.
In the following description, detailed method steps and/or structures are presented in order to provide a thorough understanding of the present invention. It will be apparent that the invention is not limited to the specific details familiar to those skilled in the art. Preferred embodiments of the present invention are described in detail below, however, the present invention may have other embodiments in addition to these detailed descriptions.
It should be understood that the present invention may be embodied in various forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. In the drawings, the size of layers and regions, as well as the relative sizes, may be exaggerated for clarity. Like numbers refer to like elements throughout.
It will be understood that the terms "comprises" and/or "comprising," when used in this specification, specify the presence of stated features, integers, steps, operations, elements, and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof. The singular forms "a", "an" and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.
In recent years, along with the rapid development of the environmental protection industry, a plurality of enterprises are actively entering the field of hazardous solid waste disposal, the hazardous solid waste in China is mainly disposed by adopting the incineration technology, along with the stricter national supervision on the environment, the standard discharge of flue gas in the incineration process is extremely important, generally, the contents of Cl and S elements in hazardous solid waste raw materials are higher, a large amount of HCl, SO 2 and other acidic gases in the flue gas are generated in the incineration process, and the wet deacidification has high removal efficiency on the HCl, SO 2 and other acidic gases in the flue gas, but the conventional wet deacidification process cannot avoid the treatment of a large amount of salt-containing wastewater, and the treatment cost and equipment investment of the part of salt-containing wastewater occupy a large proportion on the hazardous solid waste operation and equipment investment, SO that the operation cost of hazardous solid waste disposal can be greatly reduced and the equipment investment can be reduced to a certain extent if the generation of the salt-containing wastewater can be avoided in the wet deacidification process.
The invention provides high-efficiency and economical wet deacidification equipment and method, which are used for overcoming the defects that the traditional wet deacidification operation is uneconomical and high-salt wastewater is difficult to treat, and are particularly suitable for the field of hazardous solid waste disposal.
The invention provides novel equipment and a method for carrying out wet deacidification on incineration flue gas, the equipment comprises a first washing tower and a second washing tower which are communicated through a pipeline, the flue gas after dust removal passes through the first washing tower and then enters the second washing tower, wherein the first washing tower comprises circulating water, the second washing tower comprises circulating saturated Na 2CO3 solution, the first washing tower is connected with sewage treatment equipment or waste materialization treatment production equipment, the circulating water in the first washing tower absorbs HCl in the flue gas and then generates hydrochloric acid, the hydrochloric acid flows to the sewage treatment equipment or waste materialization treatment production equipment so as to be used for adjusting the pH value of the solution in the sewage treatment equipment or waste materialization treatment production equipment, the second washing tower is connected with a precipitation centrifugal separation device, and the precipitation centrifugal separation device separates salt generated by the reaction of saturated Na 2CO3 solution and acid gas in the flue gas in a solid state, and liquid obtained after precipitation and centrifugal dehydration is returned to the second washing tower.
The invention provides a high-efficiency and economical wet deacidification device and a method, wherein the wet deacidification method is characterized in that on one hand, hydrochloric acid is prepared from absorbed HCl in a first-stage washing tower and is used for a sewage treatment system to adjust pH; on the other hand, saturated Na 2CO3 solution is adopted in the secondary washing tower to further remove HCl and SO 2 in the flue gas, and simultaneously, solid waste salt is obtained in a mode of separating out NaCl and Na 2SO3 by controlling conditions in the process, SO that the generation of high-salt wastewater is avoided.
Compared with the prior art, the invention has the following advantages:
1. The invention prepares the hydrochloric acid by absorbing HCl in the flue gas, is used for adjusting the pH value of a sewage treatment system and a physical and chemical treatment production line, changes waste into valuable and reduces the operation cost.
2. The solid waste salt is obtained by adopting the way of separating out NaCl and Na 2SO3, so that the generation of high-salt-content waste water in the traditional wet deacidification process is avoided.
3. The invention adopts saturated Na 2CO3 solution to further absorb acid gas, and compared with the traditional method adopting NaOH solution for absorption, the cost of Na 2CO3 raw material is lower and more economic.
As shown in fig. 1, in one embodiment of the present invention, there is provided an apparatus 100 for wet deacidification of incineration flue gas, wherein the apparatus 100 includes a first scrubber 110 and a second scrubber 120 connected by a pipeline, and the flue gas after dust removal passes through the first scrubber 110 and then enters the second scrubber 120.
In one example, the first scrubber 110 includes recycled water and the second scrubber 120 includes recycled saturated Na 2CO3 solution. Of course, those skilled in the art will recognize that the solutions in the first scrubber 110 and the second scrubber 120 may be of other types.
The first scrubber 110 is connected to a sewage treatment plant 111 and/or a waste disposal production plant (not shown). The circulating water in the first scrubber 110 absorbs HCl in the flue gas to generate hydrochloric acid, which flows to the sewage treatment plant 111 or the waste materialization treatment production plant for adjusting pH of a solution in the sewage treatment plant 111 or the waste materialization treatment production plant.
In one example, the apparatus 100 further includes a first scrubber 110 and a wastewater treatment facility
An acid solution storage tank 113 between the disposal facility or the waste materialization disposal production facility. In one example, a valve is provided in the line between the first scrubber 110 and the acid reservoir 113.
In one example, the apparatus 100 further includes a first filter 114, a first circulation pump 115, and a second circulation pump 116 disposed outside the first scrubber 110.
One end of the first filter 114 is communicated with the interior of the first scrubber 110, the other end is communicated with the first circulating pump 115, the first circulating pump 115 is communicated with the interior of the first scrubber 110, and circulating water in the first scrubber 110 passes through the first filter 114 and is pumped into the first scrubber 110 via the first circulating pump 115 to form a water circulation, thereby achieving better absorption of acid gas.
One end of the second circulation pump 116 is connected to the inside of the first washing tower 110, and the other end is connected to the industrial water supply device 117 to replenish the industrial water into the first washing tower 110. In one example, the industrial water comes from outside the world.
In one example, a valve is disposed in the line between the first circulation pump 115 and the first scrubber 110. In one example, a valve is provided on the line between the second circulation pump 116 and the first scrubber 110.
When the pH of the circulating liquid is lower than 3, the in-column circulating liquid (circulating water) of the first scrubber 110 is discharged to the acid solution storage tank 113 while the second circulating pump 116 is turned on to replenish the industrial water. The acid solution tank 113 is used for pH adjustment of solutions in sewage treatment or other facilities of a factory such as a waste materialization disposal line.
In one example, the apparatus 100 further includes a second filter 121, third and fourth circulation pumps 122 and 123, and a saturated Na 2CO3 solution supply 124 disposed outside the second scrubber 120.
One end of the second filter 121 communicates with the interior of the second scrubber 120, and the other end communicates with the third circulation pump 122. The third circulation pump 122 is in communication with the interior of the first scrubber 110, and the circulating saturated Na 2CO3 solution in the second scrubber 120 passes through the second filter 121 and is pumped into the first scrubber 110 via the third circulation pump 122 to form a circulating saturated Na 2 CO3 solution, thereby achieving better absorption of acid gases.
The saturated Na 2CO3 solution supply 124 is in line communication with the second scrubber 120 to provide a saturated Na 2CO3 solution to the second scrubber 120. In one example, the saturated Na 2CO3 solution comes from outside the bound.
In one example, a valve is disposed in the line between the third circulation pump 122 and the first scrubber 110. In one example, a valve is provided on the line between the fourth circulation pump 123 and the first scrubber 110.
In one example, the second filter 121 is a polytetrafluoroethylene-lined basket filter.
In one example, when the pH of the circulating liquid is below 10, the saturated Na 2CO3 solution is replenished from the outside.
In one example, the apparatus 100 further comprises a sedimentation centrifugation apparatus 130. In one example, the second scrubber 120 is coupled to a precipitation centrifugal separation device 130, and the precipitation centrifugal separation device 130 precipitates salts produced by the reaction of the saturated Na 2CO3 solution with the acid gases in the flue gas in the solid state.
One end of the fourth circulation pump 123 is connected to the inside of the second washing tower 120, and the other end is connected to the sedimentation centrifugal separation device 130.
In one example, the sedimentation centrifugal separation device 130 includes a sedimentation device 131 and a centrifugal device 132. In one example, the sedimentation centrifugal separation device 130 further comprises a secondary liquid device 133.
In one example, the settling device 131 is connected to the bottom of the second scrubber 120, the centrifugal device 132 is connected to the settling device 131, the waste salt at the bottom of the second scrubber 120 is discharged to the settling device 131, and the solid waste obtained after settling is discharged to the centrifugal device 132, and is centrifugally dewatered by the centrifugal device 132. In one example, one end of the secondary liquid device 133 is connected to the settling device 131 and the centrifugal device 132, respectively, and the other end is connected to the fourth circulation pump 123, and the liquid obtained after the waste is settled in the settling device 131 and the liquid obtained after the centrifugal dehydration by the centrifugal device 132 enter the secondary liquid device 133 and are pumped into the second washing tower 120 via the fourth circulation pump 123.
In one example, the settling device 131 comprises a settling tank and/or the centrifugal device 132 comprises a centrifuge and/or the secondary liquid device 133 comprises a circulating caustic tank.
In one example, the second scrubber 120 discharges the bottom waste to the settling tank in a continuous blowdown manner, the liquid from which the settling tank is allowed to stand and separate overflows to a circulating caustic tank, the solids from which the settling tank is allowed to stand and separate are passed to a centrifuge, centrifuged by the centrifuge, the solid waste salt is disposed of by being sent out, the liquid is passed to the circulating caustic tank, and the caustic solution from the circulating caustic tank is sprayed back to the second scrubber 120 by a fourth circulation pump 123. The flue gas outlet temperature of the second scrubber 120 is maintained at 70-100 c throughout the process.
In one example, the precipitation tank is lined with a ceramic of titanium or carbon steel; the circulating alkali liquor tank is made of high-temperature glass fiber reinforced plastic.
Example 1
The main acid gas of the dedusted flue gas comprises the components of 8000mg/Nm 3、SO2 of HCl and 2000mg/Nm 3, and enters a first washing tower 110, and the circulating liquid is pumped into the first washing tower 110 by a first filter 114 by a first circulating pump 115 to absorb acid liquid; when the pH of the circulating liquid is lower than 3, the in-column circulating liquid is discharged to an acid solution storage tank 113 (spent acid storage tank) while the second circulating pump 116 is turned on to replenish the industrial water. An acid solution tank 113 (waste acid tank) is used for sewage treatment or other facilities of a factory such as a waste materialization disposal line for adjusting pH.
The flue gas scrubbed by the first stage scrubber 110 enters the second scrubber 120. The circulating liquid is pumped into the second washing tower 120 by the third circulating pump 122 through the second filter 121 to absorb the acid liquid, and when the pH of the circulating liquid is lower than 10, the saturated Na 2CO3 solution is supplemented from the outside. The second washing tower 120 adopts a continuous pollution discharge mode, the bottom waste is discharged to a settling tank, the liquid which is subjected to standing separation of the settling tank is overflowed to a circulating alkali liquid tank, the solid which is subjected to standing separation of the settling tank is delivered to a centrifugal machine, centrifugal dehydration is carried out by the centrifugal machine, the solid waste salt is delivered to be disposed, the liquid is delivered to the circulating alkali liquid tank, and the alkali liquid of the circulating alkali liquid tank is sprayed back to the second washing tower 120 through a fourth circulating pump 123. The flue gas outlet temperature of the second scrubber 120 should be maintained at 70 ℃ during the whole process, and the HCl content of the flue gas at the outlet of the second scrubber 120 is 5mg/Nm 3、SO2 and the HCl content of the flue gas at the outlet of the second scrubber is 20mg/Nm 3.
Example two
The main acid gas of the dedusted flue gas comprises HCL with the content of 8000mg/Nm 3、SO2 and 12000mg/Nm 3, and enters a first washing tower 110, and the circulating liquid is pumped into the first washing tower 110 by a first filter 114 through a first circulating pump 115 to absorb acid liquid; when the pH of the circulating liquid is lower than 3, the in-column circulating liquid is discharged to an acid solution storage tank 113 (spent acid storage tank) while the second circulating pump 116 is turned on to replenish the industrial water. An acid solution tank 113 (waste acid tank) is used for sewage treatment or other facilities of a factory such as a waste materialization disposal line for adjusting pH.
The flue gas scrubbed by the first stage scrubber 110 enters the second scrubber 120. The circulating liquid is pumped into the second washing tower 120 by the third circulating pump 122 through the second filter 121 to absorb the acid liquid, and when the pH of the circulating liquid is lower than 10, the saturated Na 2CO3 solution is supplemented from the outside. The second washing tower 120 adopts a continuous pollution discharge mode, the bottom waste is discharged to a settling tank, the liquid which is subjected to standing separation of the settling tank is overflowed to a circulating alkali liquid tank, the solid which is subjected to standing separation of the settling tank is delivered to a centrifugal machine, centrifugal dehydration is carried out by the centrifugal machine, the solid waste salt is delivered to be disposed, the liquid is delivered to the circulating alkali liquid tank, and the alkali liquid of the circulating alkali liquid tank is sprayed back to the second washing tower 120 through a fourth circulating pump 123. The flue gas outlet temperature of the second scrubber 120 should be maintained at 70 deg.c throughout the process, and the HCl content of the flue gas at the outlet of the second scrubber 120 is 5mg/Nm 3、SO2 and 40mg/Nm 3.
The invention also discloses a method for carrying out wet deacidification on incineration flue gas, which adopts the equipment of any one of the above steps, as shown in fig. 2, and comprises the following steps:
1) Introducing the flue gas after dust removal into the first washing tower 110, discharging part of the circulating water in the first washing tower 110 to an acid solution storage tank when the pH of the circulating water in the first washing tower 110 is lower than 3, and simultaneously opening a second circulating pump 116 outside the first washing tower 110 to supplement industrial water;
2) The flue gas from the first scrubber 110 enters the second scrubber 120, and the saturated Na 2CO3 solution is pumped into the second scrubber 120 by a third circulation pump 122 external to the second scrubber 120; and
3) The second washing tower 120 adopts a continuous pollution discharge mode, waste in the second washing tower 120 is discharged to the sedimentation device 131, solid waste and liquid are obtained after the waste is sedimented by the sedimentation device 131, the solid waste enters the centrifugal device 132, and the liquid returns to the second washing tower 120.
The invention provides novel equipment and a method for carrying out wet deacidification on incineration flue gas, the equipment comprises a first washing tower and a second washing tower which are communicated through a pipeline, the flue gas after dust removal passes through the first washing tower and then enters the second washing tower, wherein the first washing tower comprises circulating water, the second washing tower comprises circulating saturated Na 2CO3 solution, the first washing tower is connected with sewage treatment equipment or waste materialization treatment production equipment, the circulating water in the first washing tower absorbs HCl in the flue gas and then generates hydrochloric acid, the hydrochloric acid flows to the sewage treatment equipment or waste materialization treatment production equipment so as to be used for adjusting the pH value of the solution in the sewage treatment equipment or waste materialization treatment production equipment, the second washing tower is connected with a precipitation centrifugal separation device, and the precipitation centrifugal separation device separates salt generated by the reaction of saturated Na 2CO3 solution and acid gas in the flue gas in a solid state, and liquid obtained after precipitation and centrifugal dehydration is returned to the second washing tower.
The invention provides a high-efficiency and economical wet deacidification device and method, which are used for overcoming the defects that the traditional wet deacidification operation is uneconomical and the high-salt wastewater is difficult to treat, and are particularly suitable for the field of hazardous solid waste disposal.
The invention provides a high-efficiency and economical wet deacidification device and a method, wherein the wet deacidification method is characterized in that on one hand, hydrochloric acid is prepared from absorbed HCl in a first-stage washing tower and is used for a sewage treatment system to adjust pH; on the other hand, saturated Na 2CO3 solution is adopted in the secondary washing tower to further remove HCl and SO 2 in the flue gas, and simultaneously, solid waste salt is obtained in a mode of separating out NaCl and Na 2SO3 by controlling conditions in the process, SO that the generation of high-salt wastewater is avoided.
Compared with the prior art, the invention has the following advantages:
1. The invention prepares the hydrochloric acid by absorbing HCl in the flue gas, is used for adjusting the pH value of a sewage treatment system and a physical and chemical treatment production line, changes waste into valuable and reduces the operation cost.
2. The solid waste salt is obtained by adopting the way of separating out NaCl and Na 2SO3, so that the generation of high-salt-content waste water in the traditional wet deacidification process is avoided.
3. The invention adopts saturated Na 2CO3 solution to further absorb acid gas, and compared with the traditional method adopting NaOH solution for absorption, the cost of Na 2CO3 raw material is lower and more economic.
Similar substitutions or variations of individual components or members in the apparatus of the present invention are intended to fall within the scope of the present invention.
The present invention has been illustrated by the above-described embodiments, but it should be understood that the above-described embodiments are for purposes of illustration and description only and are not intended to limit the invention to the embodiments described. In addition, it will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that many variations and modifications are possible in light of the teachings of the invention, which variations and modifications are within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (7)
1. The wet deacidification equipment is used in an incineration flue gas purification process and is characterized by comprising a first washing tower and a second washing tower which are communicated through a pipeline, a first filter, a first circulating pump and a second circulating pump which are arranged outside the first washing tower, a second filter, a third circulating pump, a fourth circulating pump and a saturated Na 2CO3 solution supply device which are arranged outside the second washing tower, and an acid solution storage tank which is arranged between the first washing tower and a sewage treatment equipment or a waste disposal production equipment, wherein the flue gas after dust removal passes through the first washing tower and then enters the second washing tower,
The first washing tower comprises circulating water, the second washing tower comprises circulating saturated Na 2CO3 solution,
One end of the first filter is communicated with the interior of the first washing tower, the other end of the first filter is communicated with the first circulating pump, the first circulating pump is communicated with the interior of the first washing tower, the solution in the first washing tower passes through the first filter and is pumped into the first washing tower through the first circulating pump,
One end of the second circulating pump is communicated with the interior of the first washing tower, the other end of the second circulating pump is connected with an industrial water supply device so as to supplement industrial water into the first washing tower,
One end of the second filter is communicated with the interior of the second washing tower, the other end of the second filter is communicated with the third circulating pump, the third circulating pump is communicated with the interior of the first washing tower, the solution in the second washing tower passes through the second filter and is pumped into the first washing tower through the third circulating pump,
One end of the fourth circulating pump is communicated with the interior of the second washing tower, the other end of the fourth circulating pump is connected with the precipitation centrifugal separation device,
The saturated Na 2CO3 solution supply device is communicated with the pipeline of the second washing tower to supply saturated Na 2CO3 solution to the second washing tower,
The first washing tower is connected with the sewage treatment equipment or the waste materialization treatment production equipment, the circulating water in the first washing tower absorbs HCl in the flue gas to generate hydrochloric acid, the hydrochloric acid flows to the sewage treatment equipment or the waste materialization treatment production equipment to be used for adjusting the pH value of the solution in the sewage treatment equipment or the waste materialization treatment production equipment,
The bottom of the second washing tower is connected with a precipitation centrifugal separation device, the saturated Na 2CO3 solution reacts with acid gas in the flue gas to generate salt, and the precipitation centrifugal separation device separates the salt in a solid state.
2. The apparatus according to claim 1, wherein the sedimentation centrifugal separation device comprises a sedimentation device and a centrifugal device,
The sedimentation device is connected with the bottom of the second washing tower, the centrifugal device is connected with the sedimentation device, waste at the bottom of the second washing tower is discharged to the sedimentation device, and solid waste obtained after sedimentation is moved to the centrifugal device and is centrifugally dehydrated by the centrifugal device to obtain solid salt.
3. The apparatus according to claim 2, wherein the sedimentation centrifugal separation device further comprises a secondary liquid device,
One end of the secondary liquid device is respectively connected with the sedimentation device and the centrifugal device, the other end of the secondary liquid device is connected with the fourth circulating pump, and liquid obtained after the waste is sedimented in the sedimentation device and liquid obtained after centrifugal dehydration of the centrifugal device enter the secondary liquid device and are pumped into the second washing tower through the fourth circulating pump.
4. The apparatus of claim 3, wherein the precipitation device comprises a precipitation tank and/or the centrifugation device comprises a centrifuge and/or the secondary liquid device comprises a circulating alkali liquid tank, the precipitation tank is made of titanium or carbon steel lined ceramic and/or the circulating alkali liquid tank is made of high-temperature glass fiber reinforced plastic.
5. The apparatus of claim 1, wherein the second filter comprises a basket filter.
6. The apparatus of claim 5, wherein the material of the liner of the basket filter comprises polytetrafluoroethylene.
7. A method of wet deacidification for use in an incineration flue gas purification process, characterized in that the method employs the apparatus of any one of the above claims 1-6, the method comprising the steps of:
1) Introducing the flue gas after dust removal into a first washing tower, discharging part of circulating water in the first washing tower to an acid solution storage tank when the pH value of circulating liquid in the first washing tower is lower than 3, and simultaneously opening a second circulating pump outside the first washing tower to supplement industrial water into the first washing tower;
2) Pumping saturated Na 2CO3 solution into the second washing tower through a third circulating pump outside the second washing tower, and absorbing acid gas in the flue gas entering the second washing tower after exiting from the first washing tower by using saturated Na 2CO3 solution; and
3) And discharging the waste in the second washing tower to a precipitation device in a continuous pollution discharge mode, wherein the solid waste and liquid obtained after the waste is precipitated by the precipitation device enter a centrifugal device for centrifugal dehydration, and the liquid obtained after the centrifugal dehydration and the liquid obtained after the precipitation are returned to the second washing tower together.
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| CN111807495A (en) * | 2020-08-05 | 2020-10-23 | 西安热工研究院有限公司 | A water quality control device and method for preventing corrosion of indirect air-cooled circulating water system |
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