CN114588753B - Device and method for treating ammonia-containing waste gas of fly ash washing system - Google Patents

Device and method for treating ammonia-containing waste gas of fly ash washing system Download PDF

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CN114588753B
CN114588753B CN202210342991.6A CN202210342991A CN114588753B CN 114588753 B CN114588753 B CN 114588753B CN 202210342991 A CN202210342991 A CN 202210342991A CN 114588753 B CN114588753 B CN 114588753B
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washing tower
ammonia
absorption
pipeline
washing
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CN114588753A (en
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周海明
商永圭
陈志刚
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China Film (Zhejiang) Environmental Protection Technology Co.,Ltd.
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Sinochem Zhejiang Membrane Industry Development Co Ltd
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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
    • B01D53/18—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
    • B01D53/46—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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/406—Ammonia
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding

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  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
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Abstract

The application discloses flying ash washing system contains ammonia exhaust treatment device and processing method. Wherein, contain ammonia waste gas resourceful treatment system includes: the collecting unit is used for collecting the ammonia-containing waste gas; the absorption unit comprises a first washing tower, a second washing tower, a first circulating pump and a second circulating pump, the first circulating pump is used for conveying the first absorption liquid in the first washing tower to the upper part of the first washing tower so as to utilize the first absorption liquid to carry out countercurrent absorption on the ammonia-containing waste gas input by the collection unit, the second circulating pump is suitable for conveying the second absorption liquid in the second washing tower to the upper part of the second washing tower so as to utilize the second absorption liquid to carry out countercurrent absorption on the waste gas input by the first washing tower, and the second circulating pump is also suitable for conveying the second absorption liquid in the second washing tower to the first washing tower so as to supplement the first absorption liquid; and the membrane concentration unit is used for concentrating the first absorption liquid, and water or diluted ammonia water generated by the membrane concentration unit is suitable for being input into the second washing tower.

Description

Device and method for treating ammonia-containing waste gas of fly ash washing system
Technical Field
The application relates to the technical field of waste incineration fly ash treatment, in particular to an ammonia-containing waste gas treatment device and method for a fly ash washing system.
Background
In recent years, incineration has been widely used as an effective measure for reducing waste. The garbage incineration power generation project which is built and put into operation in China reaches 610 seats by 2019, the daily treatment capacity reaches 64.2 ten thousand tons, the proportion of the garbage incineration power generation project to the harmless treatment total amount of urban household garbage in China exceeds 54 percent, and the total built and put into operation of the garbage incineration power plant project in China at the end of 2020 is expected to exceed 650 seats.
In the flue gas purification process of waste incineration, ammonia water or urea is usually adopted to carry out denitration reaction on flue gas, so that a large amount of ammonia is absorbed in a pore structure of fly ash, excessive ammonia can generate heavy metal ammonium salt compounds in the fly ash semi-dry desulfurization process, most fly ash heavy metal stabilizing agents used in China at present are dithiocarbamate substances, and the substances exist in fly ash.
The disposal of the fly ash is divided into two modes of landfill and resource utilization. Resource utilization is a new treatment mode developed in recent years, for example, a cement kiln co-treatment technology is to wash fly ash (chloride is removed) to serve as a cement raw material, burn the fly ash at high temperature in a cement kiln to completely decompose dioxin, solidify and stabilize heavy metals in cement clinker, and treat and recycle all water washing wastewater. Before the fly ash is recycled, the fly ash needs to be properly pretreated, the pretreatment technology of the fly ash mainly comprises washing, solidification/stabilization, high-temperature sintering, high-temperature melting, low-temperature pyrolysis and the like, and in order to exert the capability of the cement kiln for cooperatively treating the waste incineration fly ash to the maximum extent, the fly ash is usually pretreated by adopting a fly ash washing dechlorination process at present.
In the fly ash washing process, after ammonium salt, fixing agent dithiocarbamate and other substances in fly ash are dissolved in water, ammonia is free to overflow into the air through washing and pH adjustment. In order to solve the problem of ammonia gas in the fly ash washing process, ensure the health of operators, reduce the corrosion of equipment pipelines in workshops and consider the recycling of ammonia gas, the ammonia gas recovery technology of the fly ash washing system needs to be developed.
The existing technologies at home and abroad mainly comprise several methods of physical absorption, chemical absorption, catalytic decomposition, catalytic aerobic decomposition and biodegradation for treating ammonia-containing waste gas.
The chemical absorption of ammonia utilizes the alkalinity of ammonia, so that the ammonia reacts with acidic substances to generate nitrogen fertilizer with low added value, and the method for purifying ammonia in industrial tail gas by chemical absorption is gradually eliminated in industrial application because the recovered solvent is generally high in volatility and strong in corrosivity.
Physical absorption is the most common technology for recovering ammonia, namely soft water or dilute ammonia water is used as an absorbent to absorb ammonia in industrial tail gas, the obtained low-concentration ammonia water is further distilled to obtain concentrated ammonia water, and then the concentrated ammonia water is rectified into concentrated ammonia gas, and the concentrated ammonia gas is pressurized and condensed to prepare liquid ammonia for utilization. The process has the disadvantages of (1) consuming a large amount of water; (2) a large amount of dilute ammonia water generated in the absorption process can be applied only by heating and concentrating to 20% ammonia water, and a large amount of energy is consumed; (3) the low recovery rate of ammonia causes the loss of a large amount of raw materials for synthesizing ammonia and urea. At the same time, the recovery of ammonia does not reduce the production cost increase caused by the loss of raw materials.
The ammonia catalytic decomposition technology is to completely decompose ammonia into N under the action of a catalyst 2 And H 2 The method is a feasible method for effectively removing ammonia and reducing environmental pollution. However, the ammonia decomposition process reported at present has many problems, such as that the ammonia decomposition needs to be carried out at high temperature, but when the temperature exceeds 1200 ℃, the vapor pressure of the catalyst is too high to accelerate the loss of the catalyst; when the temperature is lower than 900 ℃, the phenomena of sulfur poisoning of the catalyst or catalyst blockage caused by ammonium salt and the like are easy to occur, the service life of the catalyst is directly influenced, the heat release amount of the ammonia decomposition reaction is large, but the ammonia decomposition reaction is not easy to recycle, the ammonia catalytic decomposition energy consumption is high, the operation cost is high, and the ammonia catalytic decomposition catalyst is not suitable for being generally used.
The catalytic aerobic decomposition of ammonia is carried out by catalytically converting ammonia into N under aerobic conditions 2 And water, the decomposition reaction can be carried out at 300 ℃, the harm of ammonia is completely eliminated, and secondary pollution is not generated, so the method is an ideal treatment technology with potential. This technique is still on theoretical research, and development of a support carrier having excellent mass and heat transfer characteristics is still on theoretical research. And the ammonia gas concentration that this method was handled is lower, and the department that is not suitable for higher concentration ammonia contains ammonia waste gas and mostly does not collect completely, and the processing of the waste gas that contains ammonia after the collection also is a big difficulty.
The gaseous membrane separation process is a permeable membrane desorption absorption process (also called as a supported gas membrane process, permeable membrane desorption absorption, gas membrane absorption or membrane absorption, also broadly called as a degassing membrane or a deamination membrane) based on a membrane contactor, and can be used as a novel high-efficiency and energy-saving wastewater treatment technology for volatile reactive solutes in an aqueous solution, such as NH 3 、HCN、H 2 S、SO 2 、CO 2 、Cl 2 、Br 2 、 I 2 And the removal, recovery, enrichment and purification of amines, phenols and the like. The gas film process combines the traditional desorption tower and the absorption tower into a whole microscopically, avoids using air to blow off, and overcomes the defects of the prior artThe membrane component is a closed system, thereby avoiding the contact of toxic gas in feed liquid and a large amount of air caused by misoperation and having no secondary pollution.
In addition, in a patent with publication number CN111530237a, an ammonia gas recovery structure and an ammonia gas recovery method for a fly ash maintenance workshop are disclosed, a washing tower is adopted for two-stage spraying absorption, but the concentration of the absorbed ammonia water is very low, and the low-concentration ammonia water is used for an SNCR system, so that a large amount of water resources and energy are wasted, and the ammonia water concentration requirement of the SNCR system cannot be met.
Disclosure of Invention
An object of the application is to provide a fly ash washing system ammonia-containing waste gas treatment device and a treatment method, which can realize the recycling of ammonia gas resources while solving the problem of ammonia gas pollution of the fly ash washing system.
In order to achieve the above object, the present application provides an ammonia-containing waste gas resourceful treatment system, including:
the collecting unit is used for collecting ammonia-containing waste gas;
the absorption unit comprises a first washing tower, a second washing tower, a first circulating pump, a second circulating pump and a discharge pump, wherein the first circulating pump is used for conveying a first absorption liquid in the first washing tower to the upper part of the first washing tower so as to perform countercurrent absorption on the ammonia-containing waste gas input by the collection unit by using the first absorption liquid, the waste gas subjected to countercurrent absorption by the first washing tower is suitable for being input into the second washing tower, the second circulating pump is suitable for conveying a second absorption liquid in the second washing tower to the upper part of the second washing tower so as to perform countercurrent absorption on the waste gas input by the first washing tower by using the second absorption liquid, the second circulating pump is further suitable for conveying the second absorption liquid in the second washing tower to the first washing tower so as to supplement the first absorption liquid, and the discharge pump is used for conveying the first absorption liquid in the first washing tower to the membrane concentration unit;
and the membrane concentration unit is used for concentrating the input first absorption liquid to obtain ammonia water with preset concentration, the ammonia water with the preset concentration is suitable for being conveyed to the SCR/SNCR denitration system, and the dilute ammonia water generated by the membrane concentration unit is suitable for being input into the second washing tower to supplement the second absorption liquid.
Furthermore, the absorption unit further comprises a fresh water conveying pipeline for conveying fresh water to the second washing tower, the fresh water comes from the fresh water without calcium and magnesium generated by the membrane processing unit of the fly ash washing system, a fresh water valve is arranged on the fresh water conveying pipeline, a second liquid level sensor is arranged in the second washing tower, and the second liquid level sensor is in signal connection with the fresh water valve, so that the fresh water valve is automatically opened and closed according to the liquid level in the second washing tower.
Furthermore, the absorption unit further comprises a liquid serial pipeline, the second circulating pump is suitable for conveying the second absorption liquid in the second washing tower to the first washing tower through the liquid serial pipeline, a serial valve is arranged on the liquid serial pipeline, a first liquid level sensor is arranged in the first washing tower, and the first liquid level sensor is in signal connection with the serial valve, so that the serial valve is automatically opened and closed according to the liquid level in the first washing tower.
Further, the second washing tower comprises a second circulation pipeline, the second circulation pump is suitable for conveying the second absorption liquid in the second washing tower to the upper part of the second washing tower through the second circulation pipeline for spraying, and a second circulation valve for controlling the flow and a second flow meter arranged behind the second circulation valve are arranged on the second circulation pipeline; the first washing tower comprises a first circulating pipeline, the first circulating pump is suitable for conveying the first absorption liquid in the first washing tower to the upper part of the first washing tower through the first circulating pipeline for spraying, and a first circulating valve for controlling flow and a first flow meter arranged behind the first circulating valve are arranged on the first circulating pipeline.
Furthermore, the absorption unit further comprises a discharge pump, a first discharge pipeline, a second discharge pipeline and a third discharge pipeline, the first discharge pipeline is communicated with the inlet of the first washing tower and the discharge pump, the second discharge pipeline is communicated with the outlet of the discharge pump and the membrane concentration unit, the third discharge pipeline is communicated with the outlet of the discharge pump and the first washing tower, and a flow regulating valve is arranged on the third discharge pipeline, so that the flow of absorption liquid entering the membrane concentration unit can be controlled by the flow regulating valve.
Further, the collection unit includes waste gas collection pipeline and fan, the fan be used for with waste gas in the waste gas collection pipeline carries extremely in proper order first scrubbing tower and the second scrubbing tower, the fan is the frequency conversion fan, the waste gas collection pipeline with be provided with pressure transmitter between the fan, pressure transmitter with fan signal connection, thereby the basis pressure transmitter's signal adjustment the amount of wind of fan.
Further, the first circulating pump and the second circulating pump adopt submerged pumps.
Further, the absorption unit further comprises a fly ash washing pipeline, and the second circulating pump is suitable for conveying the second absorption liquid in the second washing tower to a fly ash washing system through the fly ash washing pipeline.
Further, the first washing tower and the second washing tower respectively comprise a demister, a spray pipe and a packing layer which are sequentially arranged in the tower body from top to bottom, the demister is used for removing liquid drops carried in gas, the spray pipe is used for spraying absorption liquid, and the packing layer is used for enabling the gas and the liquid to be fully contacted.
Further, the membrane concentration unit comprises an ammonia water conveying pipeline, ammonia water obtained through concentration is suitable for being input into the SCR/SNCR denitration system through the ammonia water conveying pipeline, and a flowmeter is arranged on the ammonia water conveying pipeline for metering.
The application also provides an ammonia-containing waste gas treatment method for the fly ash washing system, which comprises the following steps:
s100, collecting ammonia-containing waste gas of a fly ash washing system;
s200, enabling the waste gas to sequentially pass through a first washing tower and a second washing tower, and absorbing ammonia in the waste gas through a first absorption liquid in the first washing tower and a second absorption liquid in the second washing tower;
s300, concentrating the first absorption liquid by using a membrane concentration unit to obtain ammonia water with preset concentration, conveying the second absorption liquid in the second washing tower to the first washing tower to supplement the first absorption liquid, and conveying water or dilute ammonia water generated by the membrane concentration unit to the second washing tower to supplement the second absorption liquid.
In step S200, the first absorption liquid in the first scrubber is delivered to the upper portion of the first scrubber for spraying so as to recycle the first absorption liquid to absorb ammonia in the exhaust gas, and the second absorption liquid in the second scrubber is delivered to the upper portion of the second scrubber for spraying so as to recycle the second absorption liquid to absorb ammonia in the exhaust gas.
Further, the method also comprises the following steps: fresh water generated by a membrane processing unit of a fly ash water washing system is conveyed to the second washing tower to supplement the second absorption liquid.
Further, the method also comprises the following steps: and conveying the second absorption liquid in the second washing tower to a fly ash washing system for utilization.
Further, the method also comprises the following steps: and ammonia water with preset concentration obtained by concentrating the membrane concentration unit is applied to an SCR/SNCR denitration system.
Compared with the prior art, the beneficial effect of this application lies in: the ammonia-containing waste gas treatment device can absorb and concentrate ammonia water with proper concentration into ammonia water, and the ammonia water can be used for an SCR/SNCR (selective catalytic reduction/selective non-catalytic reduction) denitration unit of a waste incineration system, so that the recycling of ammonia-containing waste gas treatment is realized; the washing tower is adopted for cyclic absorption, water used for absorption comes from the production of filtered fly ash washing membranes, ammonia-containing waste gas is subjected to absorption treatment and then is discharged after reaching the standard, and a small amount of water with low ammonia content can be conveyed to the fly ash washing workshop section, so that the discharge of the ammonia-containing waste gas and wastewater after reaching the standard in the whole process is ensured; this application adopts gaseous state membrane separation technique to carry out the aqueous ammonia concentration, energy saving and consumption reduction.
Drawings
FIG. 1 is a schematic view of an embodiment of an ammonia-containing exhaust gas treatment device of a fly ash washing system;
FIG. 2 is a partial schematic view of an embodiment of an ammonia-containing exhaust gas treatment device of a fly ash water scrubbing system;
FIG. 3 is a partial schematic view of an embodiment of an ammonia-containing exhaust gas treatment device of a fly ash water scrubbing system;
in the figure: 100. a collection unit; 101. an exhaust gas collection conduit; 102. a fan; 103. a pressure transmitter; 200. an absorption unit; 211. a first scrubber; 212. a first circulation pump; 213. a first circulation pipe; 214. a first circulation valve; 215. a first flow meter; 221. a second scrubber; 222. a second circulation pump; 223. a second circulation pipe; 224. a second circulation valve; 225. A second flow meter; 231. a fresh water delivery pipeline; 232. a fresh water valve; 233. a second liquid level sensor; 234. a fresh water flow meter; 241. a liquid series line; 242. a series valve; 243. a first liquid level sensor; 251. washing the pipeline with fly ash; 261. A gas series line; 271. a discharge pump; 272. a first discharge pipe; 273. a second discharge pipe; 274. a third discharge pipe; 275. A flow regulating valve; 202. a demister; 203. a shower pipe; 204. a packing layer; 300. a membrane concentration unit; 400. a fly ash washing system; 500. a membrane processing unit; 600. a denitration system; 700. and (4) a chimney.
Detailed Description
The present application is further described below with reference to specific embodiments, and it should be noted that, without conflict, any combination between the embodiments or technical features described below may form a new embodiment.
In the description of the present application, it should be noted that, for the terms of orientation, such as "central", "lateral", "longitudinal", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc., indicate orientations and positional relationships based on the orientations or positional relationships shown in the drawings, which are only for convenience of description and simplification of the description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and should not be construed as limiting the specific scope of the present application.
It is noted that the terms first, second and the like in the description and in the claims of the present application are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order.
The terms "comprises," "comprising," and "having," and any variations thereof, in the description and claims of this application, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
The application provides a fly ash washing system contains ammonia exhaust treatment device, including collection unit 100, absorption unit 200 and concentrated unit 300 of membrane.
The collection unit 100 is used for collecting the ammonia-containing exhaust gas generated by the fly ash washing system 400. It is understood that the ammonia-containing exhaust gas can be, but is not limited to, the canister breath exhaust of the fly ash water wash system 400, the unorganized exhaust of the water basin, the non-condensable gases of the evaporation system.
The absorption unit 200 includes a first washing tower 211, a second washing tower 221, a first circulation pump 212, and a second circulation pump 222; the first circulating pump 212 is used for conveying the first absorption liquid at the bottom of the first washing tower 211 to the upper part of the first washing tower 211 for spraying, so that the ammonia-containing waste gas input by the collection unit 100 is subjected to countercurrent absorption by the first absorption liquid, and the countercurrent absorbed waste gas is suitable for being input into the second washing tower 221; the second circulation pump 222 is adapted to deliver the second absorption liquid at the bottom of the second washing tower 221 to the upper part of the second washing tower 221 for spraying, so as to perform countercurrent absorption on the exhaust gas input by the first washing tower 211 by using the second absorption liquid, and the second circulation pump 222 is further adapted to deliver the second absorption liquid to the first washing tower 211 to supplement the first absorption liquid. The absorption unit 200 operates on the following principle: the exhaust gas with higher ammonia concentration is firstly conveyed to the first washing tower 211 for countercurrent absorption, and the exhaust gas is absorbed by the first washing tower 211 and then continuously absorbed by the second washing tower 221 to fully absorb ammonia in the exhaust gas, so that the ammonia content in the finally discharged exhaust gas meets the emission standard; meanwhile, the absorption liquid used by the first washing tower 211 comes from the second washing tower 221, and the concentration of the ammonia in the exhaust gas after being absorbed by the first absorption liquid in the first washing tower 211 is higher than that of the second absorption liquid in the second washing tower 221, which is equivalent to the realization of the primary concentration of the ammonia water.
The membrane concentration unit 300 is used for concentrating the first absorption liquid in the first washing tower 211 to obtain ammonia water with a preset concentration, and water or dilute ammonia water generated by concentration of the membrane concentration unit 300 is suitable for being input into the second washing tower 221.
The application provides a processing apparatus mainly contains ammonia waste gas's processing to flying dust washing system 400, collects through collection unit 100 and contains ammonia waste gas, absorbs the ammonia in aqueous through absorption unit 200 again, improves ammonia water concentration through membrane concentration unit 300 at last, for example, concentration improves to 20%, and the ammonia water of high concentration can directly be applied to the SCR/SNCR deNOx systems 600 of msw incineration device. The treatment device organically combines the waste gas collection treatment, the membrane absorption concentration and denitration system and the fly ash washing system 400, and realizes the cyclic utilization of ammonia and water; the treatment device does not need to introduce new medicaments, does not increase new impurities, and is green and economical; the treatment device does not need traditional absorption and steam stripping, does not need a large amount of fresh water and steam, and saves water resources and steam energy to the maximum extent.
The fresh water required by the second washing tower 221 is from the membrane concentration unit 300 on one hand and also from the membrane treatment unit 500 of the fly ash water washing system 400 on the other hand, so that the water resource can be better recycled. In addition, the fresh water from the membrane treatment unit 500 is subjected to hardness removal, so that the scaling and blockage of pipelines in the SCR/SNCR denitration system 600 caused by the precipitation of calcium and magnesium ions can be well prevented, and if the washing tower adopts common tap water to absorb ammonia gas to form ammonia water, the hardness of the absorption liquid is too high, so that the blockage of the SCR/SNCR denitration system 600 is caused.
Further, the second circulation pump 222 is also adapted to convey the second absorption liquid in the second washing tower 221 to the fly ash washing system 400, so as to realize the utilization of water resources.
In some embodiments, the collecting unit 100 includes an exhaust gas collecting pipeline 101 and a fan 102, and the fan 102 is configured to sequentially convey the exhaust gas in the exhaust gas collecting pipeline 101 to the first scrubber 211 and the second scrubber 221, that is, the fan 102 is configured to overcome a resistance of the exhaust gas containing ammonia in the scrubber and realize a flow of the exhaust gas containing ammonia in the scrubber.
Further, the fan 102 is a variable frequency fan, a pressure transmitter 103 is arranged between the exhaust gas collecting pipeline 101 and the fan 102, and the pressure transmitter 103 is in signal connection with the fan 102, so that the air volume of the fan 102 can be adjusted according to the signal of the pressure transmitter 103. By signal coupling the pressure transmitter 103 to the fan 102, the collecting effect of the collecting system 100 can be ensured.
In some embodiments, the absorption unit 200 further comprises a fresh water pipeline 231 for inputting fresh water into the second washing tower 221, a fresh water valve 232 is disposed on the fresh water pipeline 231, a second liquid level sensor 233 is disposed in the second washing tower 221, and the second liquid level sensor 233 is in signal connection with the fresh water valve 232, so as to automatically switch the fresh water valve 232 according to the liquid level data of the second liquid level sensor 233. It can be understood that, since the second absorption liquid in the second scrubber tower 221 is delivered to the first scrubber tower 211 through the second circulation pump 222, the liquid level in the second scrubber tower 221 becomes low, when the liquid level in the second scrubber tower 221 is lower than the first preset value, the fresh water valve 232 is opened, fresh water enters the second scrubber tower 221 to supplement the absorption liquid, and when the liquid level in the second scrubber tower 221 reaches the second preset value, the fresh water valve 232 is closed.
Further, the fresh water pipe 231 is provided with a fresh water flow meter 234, and the fresh water flow meter 234 measures the amount of water entering the second scrubber 221.
It should be noted that the produced water of the membrane concentration unit 300 may be directly input into the second scrubber, or may be first transmitted to the fresh water transmission pipeline 231 and then input into the second scrubber 221 through the fresh water transmission pipeline 231, so that the input liquid of the membrane concentration unit 300 may be controlled.
Further, the second scrubber 221 includes a second circulation pipe 223, the second circulation pump 222 is adapted to deliver the second absorption liquid to the upper portion of the second scrubber 221 through the second circulation pipe 223, and a second circulation valve 224 and a second flow meter 225 disposed after the second circulation valve 224 are disposed on the second circulation pipe 223, so that the flow rate is controlled by the second circulation valve 224 to ensure that the flow rate of the second scrubber 221 reaches a design value.
The first scrubber 211 includes a first circulation pipe 213, the first circulation pump 212 is adapted to deliver the first absorption liquid to the upper portion of the first scrubber 211 through the first circulation pipe 213, and the first circulation pipe 213 is provided with a first circulation valve 214 and a first flow meter 215 disposed after the first circulation valve 214, so that the flow rate is controlled by the first circulation valve 214 to ensure that the flow rate of the first scrubber 211 reaches a design value.
Further, the first flow meter 215 and the second flow meter 225 are rotameters.
Further, first circulating pump 212 and second circulating pump 222 adopt submerged pump, and it can set up on the water tank of first scrubbing tower 211 and second scrubbing tower 221, so set up, are favorable to improving overall structure's compactedness, can avoid using the big, the scene of area that the centrifugal pump leads to run the condition of causing the drip.
Further, the absorption unit 200 further comprises a liquid serial pipeline 241, the second circulation pump 222 is adapted to deliver the second absorption liquid to the first washing tower 211 through the liquid serial pipeline 241, a serial valve 242 is disposed on the liquid serial pipeline 241, a first liquid level sensor 243 is disposed in the first washing tower 211, and the first liquid level sensor 243 is in signal connection with the serial valve 242, so as to automatically switch the serial valve 242 according to the liquid level data of the first liquid level sensor 243. It can be understood that, since the first absorption liquid in the second scrubber 221 is transferred to the membrane concentration unit 300, the liquid level in the first scrubber 211 becomes low, when the liquid level in the first scrubber 211 is lower than a certain preset value, the series valve 242 is opened, the second absorption liquid in the second scrubber 221 enters the first scrubber 211 to supplement the absorption liquid, and when the liquid level in the first scrubber 211 is higher than a certain preset value, the series valve 242 is closed.
In some embodiments, the absorption unit 200 further comprises a fly ash water wash pipe 251, and the second circulation pump 222 is adapted to convey the second absorption liquid to the fly ash water wash system 400 through the fly ash water wash pipe 251. It should be noted that the second absorption liquid in the second washing tower 221 is ammonia water with a very low concentration, which can be input into the fly ash washing system 400 for recycling, and then filtered by the membrane processing unit 500 of the fly ash washing system 400 to obtain fresh water, which can be input into the second washing tower 221 for ammonia absorption.
The first washing tower 211 and the second washing tower 222 respectively comprise a demister 202, a spray pipe 203 and a filler layer 204 which are sequentially arranged in the tower body from top to bottom, the demister 202 is used for removing liquid drops carried in gas, the spray pipe 203 is used for spraying absorption liquid, and the filler layer 204 is used for enabling gas and liquid to fully contact.
The demister 202 may be a commercially available demister, or a demister of a special design, for example, a demister structure of a washing tower disclosed in publication No. CN 211585721U.
In some embodiments, the center of the shower pipe 203 is provided with a nozzle, and the nozzle is a BETE high-efficiency nozzle. The spray pipe 203 and the nozzles adopt detachable structures so as to be convenient to disassemble, assemble and maintain.
In some embodiments, the bottom of the packing layer 204 is a packing support grid, the packing on the upper portion of the support grid is taylor rosette packing, and after the packing is filled with the packing, a packing pressing grid plate is installed above the packing, so that the packing is prevented from loosening and jumping under the action of high-speed airflow to influence the absorption effect. Manholes are arranged at the upper part and the bottom of the packing layer 204, so that the packing can be conveniently loaded and unloaded.
The first scrubber 211 comprises a gas series pipe 261, the gas series pipe 261 is used for conveying gas passing through a demister of the first scrubber 211 to below a packing layer of the second scrubber 221, so that waste gas absorbed through the first scrubber 211 is continuously absorbed in the second scrubber 221.
Further, the absorption unit 200 further comprises a discharge pump 271, and the discharge pump 271 is used for conveying the first absorption liquid in the first washing tower 211 to the membrane concentration unit 300.
In some embodiments, the absorption unit 200 includes a first discharge pipe 272, a second discharge pipe 273, and a third discharge pipe 274, the first discharge pipe 272 communicates with the first washing tower 211 and the inlet of the discharge pump 271, the second discharge pipe 273 communicates with the outlet of the discharge pump 271 and the membrane concentration unit 300, the third discharge pipe 274 communicates with the outlet of the discharge pump 271 and the first washing tower 211, and a flow regulating valve 275 is disposed on the third discharge pipe 274, so that the flow entering the membrane concentration unit 300 can be controlled by the flow regulating valve 275. When the concentration of the absorption liquid at the outlet of the discharge pump 271 is low, a part of the absorption liquid circulates back to the first washing tower 211 through the third discharge pipe 274, and the flow rate of the circulation is automatically adjusted by the flow adjusting valve 275.
The high concentration ammonia water obtained by the membrane concentration unit 300 is suitable for being transported to the SCR/SNCR denitration unit 600 through a pipeline. The water or low-concentration ammonia water produced by the membrane concentration unit 300 is suitable for being transferred to the second scrubber 221 through a pipe.
In one embodiment, the membrane concentration unit 300 includes an ammonia water delivery pipeline, and the concentrated ammonia water is suitable for being input into the SCR/SNCR denitration system 600 through the ammonia water delivery pipeline, and a flow meter is disposed on the ammonia water delivery pipeline for metering.
It is worth mentioning that the membrane concentration unit 300 employs a gaseous membrane separation technique to concentrate the ammonia water.
The gas discharged from the top of the second scrubber 221 is adapted to be discharged into the stack 700 through a pipe.
Compared with the prior art, the beneficial effect of this application lies in: the ammonia-containing waste gas treatment device can absorb and concentrate ammonia water with proper concentration into ammonia water, and the ammonia water can be used for an SCR/SNCR (selective catalytic reduction/selective non-catalytic reduction) denitration unit of a waste incineration system, so that the recycling of ammonia-containing waste gas treatment is realized; the washing tower is adopted for cyclic absorption, water used for absorption comes from the production of filtered fly ash washing membranes, ammonia-containing waste gas is subjected to absorption treatment and then is discharged after reaching the standard, and a small amount of water with low ammonia content can be conveyed to the fly ash washing workshop section, so that the discharge of the ammonia-containing waste gas and wastewater after reaching the standard in the whole process is ensured; this application adopts gaseous state membrane separation technique to carry out the aqueous ammonia concentration, energy saving and consumption reduction.
In one embodiment, the concentration of ammonia in the ammonia-containing exhaust gas collected by the collection unit 100 is 200mg/m 3 After the absorption in the first scrubber 211 and the second scrubber 221, the concentration of ammonia gas in the exhaust gas is 10mg/m 3 The second washing tower 221 discharges dilute ammonia water having a concentration of less than 5mg/L from the fly ash washing pipe 251, and the membrane concentration unit 300 obtains ammonia water having a concentration of 20% by weight, which can be applied to the denitration system. The treatment device not only solves the problem of ammonia pollution of the fly ash washing system, but also can realize the cyclic utilization of resources.
It is worth mentioning that the absorption unit 200 of the present application is not limited to only include the first scrubber and the second scrubber, and may include more scrubbers, and the multiple scrubbers are connected in series to improve the absorption efficiency of ammonia in the exhaust gas.
The application also provides an ammonia-containing waste gas treatment method for the fly ash washing system, which comprises the following steps:
s100, collecting ammonia-containing waste gas of a fly ash washing system;
s200, allowing the exhaust gas to sequentially pass through the first scrubber 211 and the second scrubber 221, so as to absorb ammonia in the exhaust gas by using a first absorption liquid in the first scrubber 211 and a second absorption liquid in the second scrubber 221;
s300, the membrane concentration unit 300 is adopted to concentrate the first absorption liquid to obtain ammonia water with a preset concentration, the second absorption liquid in the second washing tower 221 is conveyed to the first washing tower 211 to supplement the first absorption liquid, and water or dilute ammonia water generated by the membrane concentration unit 300 is conveyed to the second washing tower 221 to supplement the second absorption liquid.
Further, in step S200, the first absorption liquid in the first scrubber 211 is delivered to the upper portion of the first scrubber 211 for spraying so as to absorb ammonia in the exhaust gas by recycling the first absorption liquid, and the second absorption liquid in the second scrubber 211 is delivered to the upper portion of the second scrubber 211 for spraying so as to absorb ammonia in the exhaust gas by recycling the second absorption liquid.
Further, the method for treating the ammonia-containing waste gas in the fly ash washing system also comprises the following steps: fresh water generated by the membrane processing unit 500 of the fly ash water washing system 400 is sent to the second scrubber 221 to replenish the second absorption liquid.
Further, the method for treating the ammonia-containing waste gas in the fly ash washing system also comprises the following steps: the second absorption liquid in the second scrubber 221 is transported to the fly ash washing system 400 for use.
Further, the method for treating the ammonia-containing waste gas in the fly ash washing system also comprises the following steps: the ammonia water of a preset concentration concentrated by the membrane concentration unit 300 is applied to the SCR/SNCR denitration system 600.
The foregoing has described the general principles, essential features, and advantages of the application. It will be understood by those skilled in the art that the present application is not limited to the embodiments described above, which are merely illustrative of the principles of the application, but that various changes and modifications may be made without departing from the spirit and scope of the application, and these changes and modifications are intended to be within the scope of the application as claimed. The scope of protection claimed by this application is defined by the following claims and their equivalents.

Claims (5)

1. The utility model provides a fly ash washing system contains ammonia exhaust treatment device which characterized in that includes:
the collecting unit is used for collecting the ammonia-containing waste gas;
the absorption unit comprises a first washing tower, a second washing tower, a first circulating pump, a second circulating pump and a discharge pump, the first circulating pump is used for conveying a first absorption liquid in the first washing tower to the upper part of the first washing tower so as to utilize the first absorption liquid to carry out countercurrent absorption on the ammonia-containing waste gas input by the collection unit, the waste gas subjected to countercurrent absorption by the first washing tower is suitable for being input into the second washing tower, the second circulating pump is suitable for conveying a second absorption liquid in the second washing tower to the upper part of the second washing tower so as to utilize the second absorption liquid to carry out countercurrent absorption on the waste gas input by the first washing tower, and the second circulating pump is also suitable for conveying the second absorption liquid in the second washing tower to the first washing tower so as to supplement the first absorption liquid, the discharge pump is used for conveying the first absorption liquid in the first washing tower to the membrane concentration unit, the absorption unit further comprises a fresh water conveying pipeline used for conveying fresh water to the second washing tower, the fresh water comes from the fresh water without calcium and magnesium generated by the membrane processing unit of the fly ash washing system, a fresh water valve is arranged on the fresh water conveying pipeline, a second liquid level sensor is arranged in the second washing tower and is in signal connection with the fresh water valve, so that the fresh water valve is automatically opened and closed according to the liquid level in the second washing tower, the absorption unit further comprises a liquid series pipeline, the second circulating pump is suitable for conveying the second absorption liquid in the second washing tower to the first washing tower through the liquid series pipeline, a series valve is arranged on the liquid series pipeline, and a first liquid level sensor is arranged in the first washing tower, the first liquid level sensor is in signal connection with the series valve so as to automatically switch the series valve according to the liquid level in the first washing tower;
the membrane concentration unit is used for concentrating the input first absorption liquid to obtain ammonia water with preset concentration, the membrane concentration unit is used for concentrating the ammonia water by adopting a gaseous membrane separation technology, the ammonia water with the preset concentration is suitable for being conveyed to an SCR/SNCR denitration system, and dilute ammonia water generated by the membrane concentration unit is suitable for being input into the second washing tower to supplement the second absorption liquid;
the absorption unit still includes first ejection of compact pipeline, second ejection of compact pipeline and third ejection of compact pipeline, first ejection of compact pipeline intercommunication first scrubbing tower with the entry of discharge pump, second ejection of compact pipeline intercommunication the export of discharge pump with the concentrated unit of membrane, third ejection of compact pipeline intercommunication the export of discharge pump with first scrubbing tower, be provided with flow control valve on the third ejection of compact pipeline, thereby the accessible flow control valve control gets into the flow of the absorption liquid of the concentrated unit of membrane.
2. The ammonia-containing waste gas treatment device of a fly ash washing system according to claim 1, wherein the second washing tower comprises a second circulation pipeline, the second circulation pump is adapted to convey a second absorption liquid in the second washing tower to the upper part of the second washing tower for spraying through the second circulation pipeline, and a second circulation valve for controlling flow and a second flow meter arranged after the second circulation valve are arranged on the second circulation pipeline; the first washing tower comprises a first circulating pipeline, the first circulating pump is suitable for conveying the first absorption liquid in the first washing tower to the upper part of the first washing tower through the first circulating pipeline for spraying, and a first circulating valve for controlling flow and a first flow meter arranged behind the first circulating valve are arranged on the first circulating pipeline.
3. The fly ash washing system of claim 1 contains ammonia exhaust treatment device, characterized in that, the collection unit includes waste gas collection pipeline and fan, the fan be used for with waste gas in the waste gas collection pipeline carry in proper order to first scrubbing tower and the second scrubbing tower, the fan is the frequency conversion fan, waste gas collection pipeline with be provided with pressure transmitter between the fan, pressure transmitter with fan signal connection to according to pressure transmitter's signal adjustment the wind pressure of fan, in order to guarantee the effect of collecting the pipeline transport.
4. The ammonia-containing exhaust gas treatment device of a fly ash washing system according to claim 1, characterized in that: the absorption unit further comprises a fly ash washing pipeline, and the second circulating pump is suitable for conveying the second absorption liquid in the second washing tower to a fly ash washing system through the fly ash washing pipeline; and the waste gas entering the second washing tower is subjected to countercurrent absorption by the second absorption liquid and then is discharged after reaching the standard through a chimney.
5. The ammonia-containing exhaust gas treatment device of a fly ash washing system according to claim 1, characterized in that: the first washing tower and the second washing tower respectively comprise a demister, a spray pipe and a packing layer which are sequentially arranged in the tower body from top to bottom, the demister is used for removing liquid drops carried in gas, the spray pipe is used for spraying absorption liquid, the packing layer is used for enabling gas and liquid to be fully contacted and absorbed, and the first circulating pump and the second circulating pump adopt submerged pumps.
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US6065306A (en) * 1998-05-19 2000-05-23 The Boc Group, Inc. Method and apparatus for purifying ammonia
CN102872685B (en) * 2012-10-19 2015-03-25 南京信息工程大学 Method and device for recovering ammonia gas from waste gas through membrane method
CN106178860A (en) * 2016-08-29 2016-12-07 金川集团股份有限公司 One utilizes continuous circulating liquid to absorb super low concentration SO2the device and method of flue gas
CN107890761A (en) * 2017-11-14 2018-04-10 合肥创想能源环境科技有限公司 A kind of method that the industrial waste gas containing ammonia is handled using membrane separation technique
US11040308B2 (en) * 2018-07-05 2021-06-22 Cummins Emission Solutions Inc. Systems and methods for purging reductant from a reductant injector
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CN111530237A (en) * 2020-05-09 2020-08-14 中国联合工程有限公司 Ammonia gas recovery structure and ammonia gas recovery method for fly ash curing workshop
CN214862376U (en) * 2020-12-31 2021-11-26 阜阳欣奕华制药科技有限公司 Ammonia gas recovery system

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