CN219168104U - Device for cooperatively removing various pollutants by using industrial flue gas ammonia absorption method - Google Patents
Device for cooperatively removing various pollutants by using industrial flue gas ammonia absorption method Download PDFInfo
- Publication number
- CN219168104U CN219168104U CN202320361474.3U CN202320361474U CN219168104U CN 219168104 U CN219168104 U CN 219168104U CN 202320361474 U CN202320361474 U CN 202320361474U CN 219168104 U CN219168104 U CN 219168104U
- Authority
- CN
- China
- Prior art keywords
- absorption
- section
- flue gas
- ammonia
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
Abstract
The utility model belongs to the technical field of industrial flue gas pollution treatment, in particular to a removing device for cooperatively removing various pollutants by an industrial flue gas ammonia absorption method, which comprises an absorption system and a post-treatment system, wherein the absorption system comprises an absorption tower and an external system, an inlet flue is arranged at the lower part of the absorption tower, and the absorption tower is provided with a concentration section, an absorption section, a washing section and a demisting section from bottom to top; an absorption circulation loop is formed between the absorption tower and an external system; the absorption circulation loop is connected with an ammonia water conveying channel; the post-treatment system is used for recycling and reutilizing slurry below the absorption tower. The utility model discloses a device for cooperatively removing various pollutants by an industrial flue gas ammonia absorption method, which uses the same ammonia absorbent to achieve the aim of cooperatively removing, greatly shortens the process flow, has low investment cost, and simultaneously has the flue gas treatment technology of cooperatively defluorinating, denitrating, decarbonizing, deacidifying and dedusting.
Description
Technical Field
The utility model belongs to the technical field of industrial flue gas pollution treatment, and particularly relates to a removal device for cooperatively removing various pollutants by an industrial flue gas ammonia absorption method.
Background
"atmospheric pollution abatement" refers to abatement activities performed by reducing atmospheric pollutant emissions or purifying air of existing atmospheric pollutants, which are of various kinds and forms, and can be classified into two main categories according to the presence status: aerosol state contaminants and gas state contaminants. The gaseous pollutants mainly comprise: sulfur oxides, nitrogen oxides, carbon oxides, hydrogen fluoride, hydrogen chloride, and the like. Sulfur dioxide is one of the important causes of acid rain formation, and nitrogen oxides have toxic effects on human beings, animals and plants, and can cause serious environmental pollution. Carbon dioxide is one of the leading causes of global temperature rise, and a 18% reduction in carbon dioxide emissions is clearly required in the "fourteen-five" planning schema. With the global trend of reducing carbon emissions, capturing and sequestering CCS (carbon capture and s t o r a g e) of carbon dioxide is one of the most popular research directions.
In various industrial production activities, the flue gas generated by the combustion of fossil fuel is the most main source of the pollutants, and the waste incineration and hazardous waste incineration flue gas also contains the pollutants. The existing treatment means are to separately treat various pollutants, such as desulfurization, denitrification, deacidification, decarbonization and the like, and different absorbents are used, so that the process flow is very complex.
Disclosure of Invention
In order to solve the technical problems, the utility model provides a removing device for cooperatively removing various pollutants by an industrial flue gas ammonia absorption method, which adopts a single-tower multistage circulating ammonia/ammonium sulfate flue gas desulfurization technology and an externally oxidized ammonia desulfurization technology to cooperatively remove sulfur, nitrogen, decarburization, deacidification and dust; the device has high degree of automation, simple operation, low running cost and improved desulfurization efficiency.
Specifically, the utility model provides a device for cooperatively removing various pollutants by an industrial flue gas ammonia absorption method, which comprises the following steps: an absorption system and a post-treatment system,
the absorption system comprises an absorption tower and an external system, an inlet flue is arranged at the lower part of the absorption tower, a concentration section, an absorption section, a washing section and a demisting section are arranged on the absorption tower from bottom to top, and an absorption circulation loop is formed between the absorption tower and the external system and used for improving desulfurization efficiency; the absorption circulation loop is connected with an ammonia water conveying channel;
the absorption system is used for carrying out collaborative desulfurization, denitration, decarburization, deacidification and dust removal on raw flue gas through an inlet flue of the absorption tower from bottom to top through a concentration section, an absorption section, a washing section and a demisting section of the absorption tower;
the post-treatment system is used for recycling and reutilizing slurry below the absorption tower.
In some technical schemes, the inlet flue is provided with an active molecule injection port with strong oxidability, and the active molecules are used for denitration; and/or the concentration section comprises at least one concentration spraying layer, and the concentration spraying layer is used for pre-washing the flue gas and reducing the temperature of the flue gas.
In some technical schemes, the absorption section is provided with a first-stage absorption section and a second-stage absorption section from bottom to top, the first-stage absorption section is provided with a first-stage absorption section liquid collector and at least one first-stage absorption spray layer, and the second-stage absorption section is provided with a second-stage absorption section liquid collector and at least one second-stage absorption spray layer;
the external system comprises an absorbent supplementing tank and an oxidation tank; the absorption circulation loop is a closed loop formed by the absorbent replenishing groove, the primary absorption spray layer and the primary absorption section liquid collector in sequence; the oxidation tank, the secondary absorption spray layer and the secondary absorption section liquid trap are closed loop to form an oxidation circulation loop, and the oxidation circulation loop is used for deep desulfurization.
In some technical schemes, outlets of the absorbent replenishing tank and the oxidation tank are respectively provided with a pH value testing device.
In some technical schemes, the absorption circulation loop is connected with the oxidation tank through an ammonium sulfite auxiliary line, and the ammonium sulfite auxiliary line is used for supplementing liquid in the oxidation tank.
In some technical schemes, the oxidation circulation loop is connected with an ammonium sulfate spraying layer through an ammonium sulfate auxiliary line, the ammonium sulfate spraying layer is positioned between the concentrating section spraying layer and the absorbing section, and the ammonium sulfate auxiliary line is used for supplementing liquid of the concentrating section and flushing the absorbing section.
In some technical schemes, the first-stage absorption section further comprises a porous distributor, and the porous distributor is positioned between the first-stage absorption section liquid collector and the first-stage absorption spray layer.
In some technical schemes, an inlet of the absorbent replenishing tank is connected with an ammonia water solution conveying channel and a potassium carbonate solution conveying channel.
In some technical schemes, the absorption section is provided with at least one stage of absorption section defroster, the absorption section defroster is located between second grade absorption spray layer and the washing section, the absorption section defroster is used for reducing the liquid drop load that gets into the washing section, reduces the production of aerosol.
In some technical schemes, the post-treatment system comprises an evaporation crystallization system and a regeneration system, wherein the evaporation crystallization system comprises a feed liquid buffer tank, and the evaporation crystallization system is used for carrying out crystallization separation of crystal salt on slurry discharged from an absorption tower;
the regeneration system comprises a heat exchanger, a regeneration tower and a lean liquor pump, wherein an inlet of the regeneration tower is connected with a feed liquid buffer tank of the evaporative crystallization system through the heat exchanger, and feed liquid returns to an absorbent replenishing tank through the lean liquor pump after decarburization of the regeneration tower is completed, so that ammonia water recycling is realized.
The technical scheme adopted by the utility model has at least the following beneficial effects:
1. the combined removal process can realize CO 2 And SO 2 、NO X The process can realize the removal of acidic substances such as HCl and the like at the same time with high efficiency, and the process can realize 99 percent of SO 2 Removal rate and 90% CO 2 The removal rate is high, the automation degree is high, the operation is simple, and the operation cost is low.
2. The ammonia desulfurization technology with external oxidation is adopted in the scheme, an absorption circulation loop is formed between the absorption tower and an external system, an ammonia water absorbent is connected with the absorption circulation loop, and the oxidation efficiency can be ensured to be more than 99% by regulating and controlling the temperature, the solution components and the concentration, so that the desulfurization efficiency is provided.
3. The scheme is characterized in that the absorption tower is further reasonably partitioned, the absorption tower is provided with a plurality of stages of circulating partitions through a layer of partition plate and a three-layer liquid collector, reasonable concentration and pH gradient distribution are formed, ammonia is prevented from escaping, and aerosol generation is reduced.
4. The scheme is further provided with the porous distributor, the porous distributor can be used for uniformly distributing the flue gas in the tower on one hand, and on the other hand, the porous distributor is provided with a layer of liquid film which is equivalent to the bubbling tower effect, so that the porous distributor has a better washing effect on dust in the flue gas.
5. The proposal further adds potassium ions into the ammonia water solution to realize decarbonization, and both the potassium carbonate and the ammonia water have decarbonizationEffect, and potassium salt can be used for crystallizing potassium sulfate to realize SO 2 And (5) load removal.
6. The post-treatment system comprises an evaporation crystallization system and a regeneration system, wherein the evaporation crystallization system is used for carrying out crystallization separation of crystal salt on slurry discharged from an absorption tower; the inlet of a regeneration tower of the regeneration system is connected with a feed liquid buffer tank of the evaporative crystallization system through a heat exchanger, and feed liquid returns to an absorbent replenishing tank through a lean liquid pump after decarburization of the regeneration tower is completed, so that ammonia water is recycled.
Drawings
For a clearer description of the technical solutions of the embodiments of the present utility model, reference will be made to the drawings and the signs used in the embodiments, and it is obvious that the drawings described below are only some embodiments of the present utility model, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a removing device for cooperatively removing multiple pollutants by an ammonia absorption method of industrial flue gas according to an embodiment of the utility model.
The meaning of the reference symbols in the figures is as follows:
100-an absorption tower, 111-an inlet flue, 112-a concentration circulating pump, 113-a concentration section spraying layer and 114-an ammonium sulfate spraying layer; 121-a primary absorption section liquid collector, 122-a porous distributor and 123-a primary absorption spray layer; 131-a secondary absorption section liquid collector, 132-a secondary absorption spray layer, 133-an absorption section demister; 141-a water washing section liquid collector and 142-a water washing spray layer; 151-three stage ridge demister;
210-an oxidation tank, 220-a secondary absorption circulating pump, 230-a pH value detection device, 240-an ammonium sulfate auxiliary line and 250-an oxidation air conveying channel;
310-an absorbent replenishing tank, 320-a primary absorption circulating pump, 330-an ammonia water solution conveying channel, 340-a potassium carbonate solution conveying channel and 350-an ammonium sulfite auxiliary line;
411-slurry discharge pump, 412-cyclone, 413-centrifugal machine, 421-feed buffer tank, 422-feed pump, 423-heat exchanger, 424-regeneration tower, 425-lean liquor pump.
Detailed Description
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the following description will explain the specific embodiments of the present utility model with reference to the accompanying drawings. It is evident that the drawings in the following description are only examples of the utility model, from which other drawings and other embodiments can be obtained by a person skilled in the art without inventive effort.
For simplicity of the drawing, only the parts relevant to the utility model are schematically shown in each drawing, and they do not represent the actual structure thereof as a product. Additionally, in order to simplify the drawing for ease of understanding, components having the same structure or function in some of the drawings are shown schematically with only one of them, or only one of them is labeled. Herein, "a" means not only "only this one" but also "more than one" case.
It should be further understood that the term "and/or" as used in this specification and the appended claims refers to any and all possible combinations of one or more of the associated listed items, and includes such combinations.
In this context, it should be noted that the term "coupled" is to be interpreted in a broad sense, unless explicitly stated and defined otherwise, as being either a fixed connection, a removable connection, or an integral connection, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
In addition, in the description of the present application, the terms "primary," "secondary," and the like are used merely to distinguish between descriptions and are not to be construed as indicating or implying relative importance.
The core technology of the single-tower multistage circulating ammonia/ammonium sulfate flue gas desulfurization is a single-tower partition multistage multi-cycle absorption washing desulfurization technology; the core equipment is an absorption tower, the absorption tower adopts a zoned multi-circulation technology, and the absorption tower is divided into a concentration section, a primary absorption section, a secondary absorption section, a water washing section and a demisting section from bottom to top through a liquid collector.
The device for removing various pollutants cooperatively by an industrial flue gas ammonia absorption method comprises an absorption system and a post-treatment system, wherein the absorption system is used for carrying out the cooperative desulfurization, denitration, decarburization, deacidification and dust removal on raw flue gas through an absorption tower inlet flue from bottom to top through an absorption tower concentration section, an absorption section, a washing section and a demisting section; the post-treatment system is used for recycling and reutilizing slurry below the absorption tower.
The subareas of the absorption tower are separated by the liquid collector, and the liquid collector collects the solution falling from the upper part of the liquid collector, namely plays a role of cutting off a streamline, but does not obstruct the up-and-down through flow of the flue gas, and the collected liquid is discharged out of the absorption tower.
Desulfurizing and decarbonizing the system in the absorption tower, then delivering slurry discharged from the absorption tower to a post-treatment system, and drying the solid to obtain a product; the liquid is sent into a regeneration tower, the regenerated liquid after analysis can be sent back to an absorbent replenishing tank for recycling, and desulfurization and decarbonization are carried out again.
Example 1
Referring to fig. 1, a removing device for cooperatively removing multiple pollutants by an ammonia absorption method of industrial flue gas is shown, and comprises an absorption system and a post-treatment system, wherein the absorption system comprises an absorption tower 100 and an external system, an inlet flue 111 is arranged at the lower part of the absorption tower 100, and the absorption tower is provided with a concentration section, an absorption section, a washing section and a demisting section from bottom to top; an absorption circulation loop is formed between the absorption tower and an external system so as to improve the desulfurization efficiency; the absorption circulation loop is connected with an ammonia water conveying passage 330. The absorption system is used for carrying out the collaborative desulfurization, the denitration, the decarbonization, the deacidification and the dust removal of the flue gas from bottom to top through the absorption tower concentration section, the absorption section, the washing section and the demisting section through the absorption tower inlet flue 111.
In a specific embodiment, at least one concentration circulating pump 112 and at least one concentration section spraying layer 113 are arranged outside the concentration section; raw flue gas enters the concentration section of the absorption tower through the inlet flue 111 of the absorption tower, the concentration spraying layer 113 is used for pre-washing the flue gas, concentrated slurry is pumped into the concentration spraying layer 113 again through the concentration circulating pump 112, the energy consumption of the flue gas is reduced reasonably, the temperature of the absorption section is controlled by reducing the temperature of the flue gas, the concentration section is used for removing most of dust carried in the raw flue gas, and the ammonium sulfate solution is concentrated and crystallized by utilizing the enthalpy of the high-temperature raw flue gas.
In a specific embodiment, the absorption section is provided with a first-stage absorption section and a second-stage absorption section from bottom to top, and the first-stage absorption section is provided with a first-stage absorption section liquid collector 121, a porous distributor 122 and a first-stage absorption spray layer 123; the secondary absorption section is provided with a secondary absorption section liquid collector 131, a secondary absorption spray layer 132 and an absorption section demister 133.
The external system comprises an oxidation circulation loop and an absorption circulation loop, wherein the oxidation circulation loop is provided with an oxidation tank 210, a secondary absorption circulation pump 220, a pH value detection device and an ammonium sulfate auxiliary line 240, and an oxidation air conveying channel 250 is connected to an inlet below the oxidation tank 210; the absorption circulation loop is provided with an absorbent replenishing tank 310, a primary absorption circulation pump 320, a pH value detection device and an ammonium sulfite auxiliary line, and the absorbent replenishing tank 310 is connected with an ammonia water solution conveying channel 330 and a potassium carbonate solution conveying channel 340.
The primary absorption section is provided with at least two primary absorption spraying layers 123 according to the indexes of the smoke pollutants, and the spraying coverage rate is at least 200%. The primary absorption spray layer solution comes from the primary absorption circulating pump 320, is absorbed in countercurrent with the flue gas, falls into the primary absorption section liquid collector 121, enters the absorbent replenishing tank 310 below the absorption tower 100 in a self-flowing mode, and is sucked and sprayed to the primary absorption spray layer 123 from the absorbent replenishing tank 310 by the primary absorption circulating pump 320 to form closed loop primary absorption circulation. An outlet of the primary absorption cycle pump 320 is provided with an ammonium sulfite sub-line 350 to replenish the solution into the oxidation tank 210. The inlet of the absorbent replenishing tank 310 is connected with an ammonia water solution conveying channel 330, a process control mode is provided, the pH value of primary absorption spraying slurry is controlled in linkage with that of ammonia addition, a higher pH value of 6-7 is formed, desulfurization efficiency is ensured, and ammonia escape caused by excessive ammonia addition is avoided. The temperature of the primary absorption section is controlled to be 40-55 ℃ by means of water supplementing and the like; the primary absorption section is used for absorbing acid pollutants in the flue gas and is used for bearing the main task of removing sulfur dioxide.
In a specific embodiment, a porous distributor 122 is arranged between a primary absorption section liquid collector 121 and a primary absorption spray layer in the absorption tower 100 to achieve the purpose of dust removal; when the flue gas passes through the spraying layer, particles with the particle size less than or equal to 2.5 mu m have a certain probability to be coagulated, grown and removed. And the liquid-holding layer on the porous distributor greatly enhances the removal effect of the particles with the particle diameter less than or equal to 2.5 mu m.
In one embodiment, the secondary absorption section is provided with at least one secondary absorption spray layer 132 with a spray coverage of at least 200%. The solution of the secondary absorption spray layer 132 comes from the secondary absorption circulating pump 220, is absorbed in countercurrent with the flue gas, falls into the secondary absorption section liquid collector 131, enters the oxidation tank 210 in a self-flowing mode, and is sucked and sprayed from the oxidation tank 210 to the secondary absorption spray layer 132 by the secondary absorption circulating pump 220 to form closed loop secondary absorption circulation. An outlet of the secondary absorption circulating pump 220 is provided with an ammonium sulfate auxiliary line 240, the ammonium sulfate spraying layer 114 is supplemented with the solution, the ammonium sulfate spraying layer 114 is positioned above the concentrated spraying layer 113, the nozzles of the ammonium sulfate spraying layer 114 are arranged in an upper layer and a lower layer, the ammonium sulfate auxiliary line is thinner, and the upward spraying can be used for flushing the liquid collector 121 of the primary absorption section; the pH of the secondary absorption solution is lower, the temperature and the pH can not influence the optimal crystallization environment (pH 2-2.5 and temperature 50-60 ℃) of the concentration section, and the quality of the ammonium sulfate byproduct is ensured; the secondary absorption section is used for oxidizing sulfite ions into sulfate ions, and simultaneously circularly washing, carrying out deep desulfurization and preventing ammonia from escaping.
In one embodiment, oxidation tank 210 in the oxidation circulation loop oxidizes sulfite to sulfate, and is fixed to avoid sulfur dioxide escape; the oxidation tank 210 is connected with the oxidation air conveying channel 250, air is blown in through the oxidation fan, the oxidation height is controlled to be at least 5m, the oxygen utilization rate is ensured to be more than 30%, and the energy consumption of the oxidation fan is saved. The oxidation efficiency can be ensured to be more than 99% by regulating and controlling the temperature, the solution composition and the concentration of the ammonium sulfite auxiliary line 350 arranged at the outlet of the primary absorption circulating pump 320, the pH value of the oxidized secondary absorption solution is 3-5, and the solution with lower pH value is arranged above the primary absorption section, so that ammonia escape and aerosol generation can be controlled. The temperature of the secondary absorption section is controlled to be 30-50 ℃ by means of water supplementing and the like.
In one embodiment, the pH detecting device 230 is provided at the outlet of the absorbent replenishing tank 310 and the oxidation tank 210, and the amount of ammonia water to be added is strictly controlled to prevent the ammonia from being excessive.
In a specific embodiment, the inlet of the absorbent replenishing tank 310 is also connected with a potassium carbonate solution conveying channel 340, and potassium ions are added into the ammonia water solution to realize decarburization; the solubility of potassium sulfate increases slowly and linearly with increasing temperature, and the solubility is smaller than other C0 2 And S0 2 Loading salts in ammonia water solution. The solubility of potassium carbonate is very high, carbonate salt can not be separated out by adding potassium salt, and the potassium sulfate is a good potassium fertilizer and has a certain economic value, so that S0 is realized by adding potassium ions into an ammonia water solution in a potassium salt crystallization mode 2 And (3) loading.
In a specific embodiment, the absorption section is further provided with at least one stage of absorption section demister 133, the absorption section demister is located between the secondary absorption spray layer 132 and the water washing section, and the absorption section demister demists the flue gas after the absorption cycle, so that the droplet load entering the water washing section is reduced. Because more ammonium sulfate is dissolved in the absorption liquid of the absorption section, the liquid drops entering the water washing section are strictly controlled, so that the total dust (containing ammonium salt) at the outlet can be ensured to reach the ultralow requirement, and the generation of aerosol is reduced. The mechanism of aerosol formation can be analyzed to find out two essential conditions for aerosol occurrence: excess ammonia and high concentration solution. The liquid for washing the demister in the absorption section of the system is process water, and continuously dilutes circulating liquid to prevent the circulating liquid from producing ammonium sulfite solid by saturated crystallization. Therefore, the secondary absorption circulation of the system has good effect on preventing the problems of excessive ammonia, crystallization of circulating liquid and the like, and aerosol is difficult to appear naturally.
In one embodiment, a multistage water washing technique is employed above the absorber stage mist eliminator 133, with a water wash stage having a water wash stage collector 141 and a water wash spray layer 142 thereonA three-stage ridge demister 151 is arranged above the demister, and the flue gas is purified to remove the flue gas and the halogen; the concentration of the mist drops at the outlet reaches 20mg/Nm 3 And the generation of ammonia escape and aerosol is reduced to the greatest extent, various pollutants such as dust, fog drops, acid fog drops and the like carried by the flue gas are deeply removed, and the ultra-low emission of clean flue gas particles at the outlet of the absorption tower is ensured.
In a specific embodiment, active molecules with strong oxidizing property are sprayed into the front inlet flue 111 of the wet absorption tower 100 at a proper position, and NOx in the flue gas is oxidized into high-valence nitrogen oxides by using the active molecules, SO that SO is realized in the desulfurizing tower 2 And NOx is integrally removed, and finally the concentration of NOx in the flue gas is reduced to below 50mg/Nm 3. The active molecules of the patent can be selected from ozone, sodium hypochlorite and the like.
In a specific embodiment, the ammonia water absorbent is sprayed into the wet absorption tower and is countercurrent to the flue gas to absorb sulfur dioxide, carbon dioxide, hydrogen chloride, hydrogen fluoride, nitrogen oxides and other substances in the flue gas.
In one embodiment, the aftertreatment system includes an evaporative crystallization system, a feed solution buffer tank 421, a feed solution pump 422, a heat exchanger 423, a regeneration tower 424, and a split solution pump 425; the evaporative crystallization system includes a slurry discharge pump 411, a cyclone 412, and a centrifugal machine 413, the discharge pump 411 and the centrifugal machine 413 being connected through the cyclone 412.
The inlet of the regeneration tower 424 is connected with an evaporation crystallization system through a medium loop of the heat exchanger 423 for decarburization; the regenerated liquid below the regeneration tower 424 is pumped into a lean liquid pump 425 and then connected with an absorption circulation loop through a medium loop II of the heat exchanger for recycling the ammonia water.
In one embodiment, the post-treatment system passes slurry below absorber 100 through slurry reject pump 411 into cyclone 412 and centrifugal machine 413 in sequence for crystallization separation of ammonium sulfate and/or potassium sulfate. The residual feed liquid after evaporation and crystallization sequentially passes through a feed liquid buffer tank 421, a feed liquid pump 422 and a heat exchanger 423 to enter a regeneration tower 424, the regeneration tower 424 is heated to realize the analysis of ammonium bicarbonate, the removed carbon dioxide can be sealed or chemically utilized or used for preparing food-grade carbon dioxide, and the ammonia water below the regeneration tower 424 is pumped into the heat exchanger 423 through a liquid separating pump 425 to enter an absorption circulation loop, so that the recovery and the reutilization of the ammonia water are realized.
The foregoing examples illustrate only a few embodiments of the utility model and are described in detail herein without thereby limiting the scope of the utility model. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the utility model, which are all within the scope of the utility model. Accordingly, the scope of the utility model should be assessed as that of the appended claims.
It should be understood by those skilled in the art that while the present utility model has been described in terms of several embodiments, not every embodiment contains only one independent technical solution. The description is given for clearness of understanding only, and those skilled in the art will understand the description as a whole and will recognize that the technical solutions described in the various embodiments may be combined with one another to understand the scope of the present utility model.
Claims (10)
1. A device for cooperatively removing various pollutants by an industrial flue gas ammonia absorption method is characterized in that: comprising an absorption system and a post-treatment system,
the absorption system comprises an absorption tower and an external system, an inlet flue is arranged at the lower part of the absorption tower, a concentration section, an absorption section, a washing section and a demisting section are arranged on the absorption tower from bottom to top, and an absorption circulation loop is formed between the absorption tower and the external system and used for improving desulfurization efficiency; the absorption circulation loop is connected with an ammonia water conveying channel,
the absorption system is used for carrying out collaborative desulfurization, denitration, decarburization, deacidification and dust removal on raw flue gas through an inlet flue of the absorption tower from bottom to top through a concentration section, an absorption section, a washing section and a demisting section of the absorption tower;
the post-treatment system is used for recycling and reutilizing slurry below the absorption tower.
2. The device for cooperatively removing a plurality of pollutants by using an industrial flue gas ammonia absorption method according to claim 1, which is characterized in that: the inlet flue is provided with an active molecule injection port with strong oxidability, and the active molecules are used for denitration; and/or the number of the groups of groups,
the concentration section comprises at least one concentration spraying layer, and the concentration spraying layer is used for pre-washing the flue gas and reducing the temperature of the flue gas.
3. The device for cooperatively removing a plurality of pollutants by using an industrial flue gas ammonia absorption method according to claim 1, which is characterized in that: the absorption section is provided with a primary absorption section and a secondary absorption section from bottom to top,
the primary absorption section is provided with a primary absorption section liquid collector and at least one primary absorption spray layer,
the secondary absorption section is provided with a secondary absorption section liquid collector and at least one secondary absorption spray layer;
the external system comprises an absorbent supplementing tank and an oxidation tank;
the absorption circulation loop is a closed loop formed by the absorbent replenishing groove, the primary absorption spray layer and the primary absorption section liquid collector in sequence;
the oxidation tank, the secondary absorption spray layer and the secondary absorption section liquid trap are closed loop to form an oxidation circulation loop, and the oxidation circulation loop is used for deep desulfurization.
4. The device for cooperatively removing a plurality of pollutants by using an ammonia absorption method of industrial flue gas according to claim 3, which is characterized in that: and the outlets of the absorbent supplementing tank and the oxidation tank are respectively provided with a pH value testing device.
5. The device for cooperatively removing a plurality of pollutants by using an ammonia absorption method of industrial flue gas according to claim 3, which is characterized in that: the absorption circulation loop is connected with the oxidation tank through an ammonium sulfite auxiliary line, and the ammonium sulfite auxiliary line is used for supplementing liquid in the oxidation tank.
6. The device for cooperatively removing a plurality of pollutants by using an ammonia absorption method of industrial flue gas according to claim 3, which is characterized in that: the oxidation circulation loop is connected with an ammonium sulfate spraying layer through an ammonium sulfate auxiliary line, the ammonium sulfate spraying layer is positioned between the concentrating section spraying layer and the absorbing section, and the ammonium sulfate auxiliary line is used for supplementing liquid of the concentrating section and flushing the absorbing section.
7. The device for cooperatively removing a plurality of pollutants by using an ammonia absorption method of industrial flue gas according to claim 3, which is characterized in that: the primary absorption section further comprises a porous distributor, and the porous distributor is positioned between the primary absorption section liquid collector and the primary absorption spray layer.
8. The device for cooperatively removing a plurality of pollutants by using an ammonia absorption method of industrial flue gas according to claim 3, which is characterized in that: the inlet of the absorbent replenishing tank is connected with an ammonia water solution conveying channel and a potassium carbonate solution conveying channel.
9. The device for cooperatively removing a plurality of pollutants by using an ammonia absorption method of industrial flue gas according to claim 3, which is characterized in that: the absorption section is provided with at least one stage of absorption section demister, the absorption section demister is located between the secondary absorption spray layer and the water washing section, and the absorption section demister is used for reducing the liquid drop load entering the water washing section and reducing the generation of aerosol.
10. The device for cooperatively removing a plurality of pollutants by using an industrial flue gas ammonia absorption method according to claim 8, which is characterized in that: the post-treatment system comprises an evaporation crystallization system and a regeneration system, wherein the evaporation crystallization system comprises a feed liquid buffer tank, and the evaporation crystallization system is used for carrying out crystallization separation of crystal salt on slurry discharged from an absorption tower;
the regeneration system comprises a heat exchanger, a regeneration tower and a lean liquor pump, wherein an inlet of the regeneration tower is connected with a feed liquid buffer tank of the evaporative crystallization system through the heat exchanger, and feed liquid returns to an absorbent replenishing tank through the lean liquor pump after decarburization of the regeneration tower is completed, so that ammonia water recycling is realized.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320361474.3U CN219168104U (en) | 2023-03-01 | 2023-03-01 | Device for cooperatively removing various pollutants by using industrial flue gas ammonia absorption method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320361474.3U CN219168104U (en) | 2023-03-01 | 2023-03-01 | Device for cooperatively removing various pollutants by using industrial flue gas ammonia absorption method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219168104U true CN219168104U (en) | 2023-06-13 |
Family
ID=86664728
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320361474.3U Active CN219168104U (en) | 2023-03-01 | 2023-03-01 | Device for cooperatively removing various pollutants by using industrial flue gas ammonia absorption method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219168104U (en) |
-
2023
- 2023-03-01 CN CN202320361474.3U patent/CN219168104U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR102302849B1 (en) | Method for controlling aerosol production during absorption in ammonia desulfurization | |
| US11224838B2 (en) | Controlling aerosol production during absorption in ammonia-based desulfurization | |
| KR102036816B1 (en) | Method and apparatus for effectively removing sulfur oxides and dust in gas by ammonia-based process | |
| JP7062509B2 (en) | Carbon capture | |
| CN102228777B (en) | Double-oxidation ammonia desulfurization process and device | |
| BR102019008222A2 (en) | acid gas treatment | |
| CN109529549A (en) | Ultra-clean ammonia-process desulfurization technique is applied to the method for carbon capture process | |
| CN103228340A (en) | Trace component removal in CO2 removal processes by means of a semipermeable membrane | |
| CN101422693A (en) | Sulphuric acid tail-gas deep desulfurization method | |
| CN113856441B (en) | Ammonia desulfurization method and ammonia desulfurization apparatus | |
| CN219168104U (en) | Device for cooperatively removing various pollutants by using industrial flue gas ammonia absorption method | |
| CN211274164U (en) | Ammonia-containing tail gas treatment device for dry ammonium workshop section in alkali industry | |
| CN202105585U (en) | Double-oxidation ammonia desulphurization device | |
| CN201823468U (en) | Twin tower ammonia desulfurization device | |
| CN103768911A (en) | Flue gas purification device and method capable of realizing desulfurization, denitrification and respective recovery | |
| CN202751945U (en) | Desulphurization and denitration device with ammonia process | |
| CN109351153A (en) | Desulfation dust-extraction device suitable for ammonia desulfurizing process | |
| CN220370777U (en) | Composite absorption tower for ultralow emission of biomass power plant | |
| CN219922524U (en) | Decarbonizing flue gas treatment system | |
| CN101844034B (en) | Device for removing sulfur dioxide from waste gas and producing ammonium sulfate byproduct | |
| JPH10230129A (en) | Flue gas desulfurization method and flue gas desulfurizing device | |
| CN117427468A (en) | Recycling system of desulfurization and decarbonization absorbent and use and flexible regulation and control method thereof | |
| SU1721155A1 (en) | Method of recovering cinder from sulfate cellulose production flue gases | |
| CN116603369A (en) | Absorbent capable of efficiently absorbing sulfur dioxide | |
| IT202000020473A1 (en) | SYSTEM AND METHOD OF ABATEMENT OF CARBON DIOXIDE BASED ON AMMONIA, AND DIRECT CONTACT COOLER FOR THEM |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |