CN217746471U - System for semidry method for flue gas purification - Google Patents
System for semidry method for flue gas purification Download PDFInfo
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- CN217746471U CN217746471U CN202221940002.5U CN202221940002U CN217746471U CN 217746471 U CN217746471 U CN 217746471U CN 202221940002 U CN202221940002 U CN 202221940002U CN 217746471 U CN217746471 U CN 217746471U
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Abstract
The utility model relates to a system for semidry method for gas cleaning relates to gas cleaning technical field, including the spray drying tower, sack reactor, desulfurization absorption tower and concentrated system, the bottom and I intercommunication in flue of spray drying tower, the well lower part and the intercommunication of concentrated system of spray drying tower, the top of spray drying tower with sack reactor intercommunication, the well lower part intercommunication of sack reactor and desulfurization absorption tower, the lower part and the concentrated system intercommunication of desulfurization absorption tower. Through adopting spray drying tower, sack reactor, desulfurization absorption tower and solution evaporative concentration system to cooperate, realized higher denitration and desulfurization's efficiency, no waste water produces, and is more environmental protection.
Description
Technical Field
The utility model relates to a flue gas purification technical field, concretely relates to system for semi-dry method of flue gas purification.
Background
With the rapid development of industrialization, the problem of atmospheric pollution is gradually highlighted. For example, flue gas generated in furnaces such as steel, cement, building materials, glass, metallurgy and the like contains a large amount of pollutants such as sulfur dioxide, nitrogen oxides, smoke dust and the like, which cause great harm to human health and ecological environment.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that a system for semidry method for gas cleaning is provided. The purpose does not use the catalyst when providing the denitration, has higher denitration desulfurization's efficiency, and no waste water produces, environmental protection, no waste material produces.
The utility model provides a solve above-mentioned technical problem, provide a system for semidry method of gas cleaning, including the spray drying tower that is arranged in making former flue gas and the mutual contact of atomizing supersaturated ammonium sulfite solution cocurrent flow for adsorb solid particle and make the cloth bag reactor that ammonium sulfite and nitrogen oxide take place to react in the solid particle, a desulfurization absorption tower for making denitration flue gas and urea solution reaction, a concentration system for making the generation liquid evaporative concentration that contains ammonium sulfite obtain supersaturated ammonium sulfite solution, and the urea that is used for providing urea solution joins in marriage the liquid device, the bottom and the I intercommunication of flue of spray drying tower, the well lower part and the intercommunication of concentration system of spray drying tower, the top of spray drying tower with cloth bag reactor intercommunication, cloth bag reactor and desulfurization absorption tower's well lower part intercommunication, the lower part and the concentration system intercommunication of desulfurization absorption tower, urea join in marriage the liquid device with the desulfurization absorption tower intercommunication.
The beneficial effect who adopts above-mentioned scheme is: through adopting spray drying tower, sack reactor, desulfurization absorption tower and solution evaporative concentration system to cooperate, realized higher denitration and desulfurization's efficiency, no waste water produces, and is more environmental protection.
Further, the cloth bag reactor comprises at least 10 cloth bag units, the bottom of each cloth bag unit is provided with a unit inlet, each unit inlet is communicated with the top of the spray drying tower through a flue II, the top of each cloth bag unit is provided with a unit outlet, and each cloth bag unit comprises at least 3 groups of communicated cloth bags. Each cloth bag unit comprises at least 3 groups of cloth bags which are communicated in series or in parallel.
The beneficial effect of adopting the further scheme is that: the dry solid particles are convenient to collect by adopting a plurality of groups of cloth bag reactors, and the solid particles are adsorbed on the surfaces of the cloth bag reactors, so that ammonium sulfite in the solid particles and nitrogen oxide in the flue gas passing through the cloth bag reactors are fully reacted.
Furthermore, each cloth bag is cylindrical, the diameter of each cloth bag is 200-300mm, and the length of each cloth bag is 8-10m.
Furthermore, communicating pipes are arranged between the adjacent cloth bag units and at the bottoms of the cloth bag units, a back-blowing air port is formed in the top of each cloth bag unit and communicated with a back-blowing fan through a back-blowing air pipeline, a pneumatic valve is arranged on the back-blowing air pipeline at the back-blowing air port, and another pneumatic valve is arranged on the unit outlet.
The beneficial effect of adopting the further scheme is that: adopt multiunit sack reactor, and be provided with communicating pipe in the bottom that just is located the sack unit between adjacent sack unit, be provided with the pneumatic valve respectively at blowback gas mouth and unit export, when sack pressure differential increase, be convenient for on the one hand carry out the blowback to the sack reactor and unload, on the other hand reduces the influence to the denitration effect of system when the sack reactor blowback.
Furthermore, the bottom of each cloth bag unit is hermetically provided with an inclination angle hopper, the bottom of each inclination angle hopper is provided with a discharging outlet, and each discharging outlet is provided with a star-shaped valve.
The beneficial effect of adopting the further scheme is that: the material storage and the material discharge are facilitated by the adoption of the inclination angle hopper, the material discharge outlet and the star-shaped valve.
Further, the spray drying tower comprises a drying tower body, a tower bottom swirler and a solution atomizer; a tower bottom swirler is arranged at the lower part in the cavity of the drying tower body, the drying tower body positioned at the lower part of the tower bottom swirler is communicated with a flue I, the drying tower body positioned at the upper part of the tower bottom swirler is communicated with one end of a pipeline I, one end of the pipeline I extends into the cavity of the drying tower body, and one end of the pipeline I is provided with a solution atomizer; the top of drying tower body is passed through flue II and sack reactor intercommunication, flue II and bypass flue one end intercommunication, be provided with the bypass valve on the bypass flue, the bypass flue other end and III intercommunications of flue, and the draught fan is located the flue III of keeping away from the bypass flue.
The beneficial effect of adopting the further scheme is that: therefore, the spray drying tower is convenient to adopt gas-liquid parallel flow contact, the original flue gas and the atomized supersaturated ammonium sulfite solution flow upwards from the lower part of the tower, the gas-liquid contact time and area are ensured, the gas-liquid phase can be strongly disturbed, the operation range is wide, the operation is stable, and the resistance is small.
Further, the desulfurization absorption tower comprises an absorption tower liquid outlet pump, an absorption tower circulating pump, a packing layer, a demister and an absorption tower body, wherein an absorption tower liquid storage chamber is arranged at the bottom of an inner cavity of the absorption tower body, the packing layer and the demister are sequentially arranged in the inner cavity of the absorption tower body above the absorption tower liquid storage chamber, the absorption tower body positioned between the absorption tower liquid storage chamber and the packing layer is communicated with a cloth bag unit through a flue III, the absorption tower liquid storage chamber is communicated with one end of a circulating pipe I, the other end of the circulating pipe I extends into the inner cavity of the absorption tower body positioned between the packing layer and the demister, an absorption tower nozzle is arranged at the other end of the circulating pipe I, the absorption tower circulating pump is arranged on the circulating pipe I, the top of the absorption tower body is communicated with a flue IV, a sulfur dioxide and nitrogen oxide analyzer is arranged on the flue IV, and a pH meter is arranged in the absorption tower liquid storage chamber.
The beneficial effect of adopting the further scheme is that: by adopting the desulfurization absorption tower, the desulfurization absorption tower is ensured to adopt gas-liquid countercurrent contact, the flue gas flows downwards from the upper part of the tower from bottom to top and is dispersed in a gas phase in a liquid drop shape, the gas and the liquid have enough contact time and area, the gas and the liquid can be strongly disturbed, the operation is stable, and the resistance is small.
Further, a draught fan is arranged on the flue III.
The beneficial effect of adopting the further scheme is that: the flue III is communicated with the bypass flue, so that the bypass flue is convenient to open when the system is started, and the bypass flue is closed after the temperature of the system rises.
Further, the concentration system comprises an evaporation liquid outlet pump, an evaporation separator, an evaporation circulating pump, a steam heater, a condenser and a water ring vacuum pump, wherein a tube pass inlet of the evaporation separator is communicated with the liquid storage chamber of the absorption tower through a pipeline II, the evaporation liquid outlet pump is arranged on the pipeline II, an outlet of a tube pass on the side wall of the evaporation separator is communicated with the drying tower body through a pipeline I, the evaporation liquid outlet pump is arranged on the pipeline I, a shell pass inlet of the evaporation separator is connected with one end of a circulating pipe II, a shell pass bottom outlet on the side wall of the bottom of the evaporation separator is connected with the other end of the circulating pipe II, the evaporation circulating pump and the steam heater are sequentially arranged on the circulating pipe II along the shell pass outlet to the shell pass inlet, a tube pass top outlet at the top of the evaporation separator is connected with the tube pass connected with the condenser through an evaporation pipe, and the tube pass of the condenser is further connected with the water ring vacuum pump.
The beneficial effect of adopting the further scheme is that: the temperature of the generated liquid containing ammonium sulfite is raised through a steam separator, the generated liquid is concentrated to reach a supersaturated state, the solid content reaches 2 to 10 percent, and then the generated liquid is sent into a spray drying tower, so that the whole system can operate conveniently.
The urea liquid preparation device comprises a liquid preparation tank, a delivery pump and a delivery pipe, wherein the liquid preparation tank is communicated with the absorption tower body through the delivery pipe, and the delivery pipe is provided with the delivery pump. The urea liquid preparation device further comprises a urea bin, a stirrer and a weighing machine, wherein the urea bin is connected with the liquid preparation tank through the weighing machine, and the stirrer is arranged in the liquid preparation tank.
The beneficial effect of adopting the further scheme is that: the urea solution with a certain mass fraction is conveniently prepared for the desulfurization absorption tower.
Furthermore, a sulfur dioxide and nitrogen oxide analyzer, a thermometer, a pressure gauge and an air gauge are sequentially installed on the flue I, and a sulfur dioxide and nitrogen oxide analyzer, a thermometer, a pressure gauge and an air gauge are sequentially installed on the flue IV; a thermometer and a pressure gauge are arranged on the flue II and the flue III according to requirements; the absorption tower is characterized in that a thermometer and a pH meter are installed on the absorption tower liquid storage chamber, and a thermometer and a pH meter are installed on the tube pass of the evaporation separator.
The beneficial effect of adopting the above further scheme is: therefore, the temperature and the pressure of the operation of the whole system are convenient to monitor; install sulfur dioxide and nitrogen oxide analysis appearance through installing at flue I and be convenient for detect the volume that contains sulphur nitre of treating the flue gas that purifies, install sulfur dioxide and nitrogen oxide analysis appearance through IV in the flue and be convenient for detect the volume that contains sulphur nitre of flue gas after purifying, be convenient for regulate and control the feed volume of former flue gas.
Drawings
FIG. 1 is a schematic view of the overall assembly of the present invention;
FIG. 2 is a schematic structural view of the cloth bag reactor of the present invention;
FIG. 3 is a schematic view of a bottom swirler of the present invention;
fig. 4 is a schematic view of the central blocking plate of the tower bottom swirler of the present invention;
fig. 5 is a schematic view of the solution atomizer of the present invention.
In the drawings, the components represented by the respective reference numerals are listed below:
1-spray drying tower, 101-tower bottom cyclone, 102-solution atomizer, 103-drying tower body, 2-cloth bag reactor, 201-cloth bag unit, 202-cloth bag, 203-unit inlet, 204-discharge outlet, 205-dip angle hopper, 206-star valve, 207-unit outlet, 208-pneumatic valve, 209-communicating pipe, 210-back blowing gas port, 211-back blowing fan, 3-draught fan, 4-desulfurization absorption tower, 401-absorption tower liquid outlet pump, 402-absorption tower circulating pump, 403-packing layer, 404-demister, 405-absorption tower body, 406-absorption tower nozzle, 407-absorption tower liquid storage chamber, 408-circulation pipe I, 5-urea liquid preparation device, 501-liquid preparation tank, 502-delivery pump, 503-urea bin, 504-weighing machine, 505-delivery pipe, 506-stirrer, 6-concentration system, 601-evaporation liquid pump, 602-evaporation separator, 603-evaporation circulating pump, 604-steam heater, 605-condenser, 606-condensed water recovery tank, 607-water ring vacuum pump, 608-circulation pipe II, 609-evaporation pipe, 7-flue I, 8-flue II, 9-bypass flue, 10-flue III, 11-flue IV, 12-pipeline I, 13-pipeline II, 14-bypass valve.
Detailed Description
The principles and features of the present invention are described below, with the examples being given only for the purpose of illustration and not for the purpose of limiting the scope of the invention.
Example 1
The embodiment relates to a semi-dry treatment method for flue gas purification, which comprises the following steps:
step 1: the raw flue gas and the atomized supersaturated ammonium sulfite solution are in parallel flow and mutually contacted, the supersaturated ammonium sulfite solution is converted into solid particles, ammonium sulfite in the solid particles reacts with nitric oxide in the raw flue gas to generate ammonium sulfate solid particles, and the raw flue gas is converted into denitration flue gas;
step 2: the denitration flue gas in the step 1 reacts with a urea solution to generate a generated liquid containing ammonium sulfite, and the denitration flue gas is converted into clean flue gas;
and step 3: and (3) evaporating and concentrating the generated solution containing the ammonium sulfite in the step (2) to obtain a supersaturated ammonium sulfite solution, and atomizing the supersaturated ammonium sulfite solution for the step (1). The main reaction equation is as follows:
2(NH 4 ) 2 SO 3 +2NO＝2(NH 4 ) 2 SO 4 +N 2 ；
4(NH 4 ) 2 SO 3 +2NO 2 ＝4(NH 4 ) 2 SO 4 +N 2 ；
CO(NH) 2 +2H 2 O＝(NH 4 ) 2 CO 3 ；
(NH 4 ) 2 CO 3 +SO 2 ＝(NH 4 ) 2 SO 3 +CO 2 ；
(NH 4 ) 2 SO 3 +H 2 O+SO 2 ＝2NH 4 HSO 3 ；
2NH 4 HSO 3 +(NH 4 ) 2 CO 3 ＝2(NH 4 ) 2 SO 3 +CO 2 +H 2 O。
no catalyst is used during the denitration through steps 1 to 3, the efficiency of denitration and desulfuration is higher, no wastewater is generated, the environment is protected, and the urea solution is finally converted into ammonium sulfate, so that the urea solution is convenient to reuse.
Wherein, the step 1 specifically comprises the following steps: the raw flue gas and the atomized supersaturated ammonium sulfite solution are firstly in parallel flow in a spray drying tower 1 to mutually contact and react for 3-10s, the supersaturated ammonium sulfite solution is converted into solid particles, and the raw flue gas is converted into the flue gas to be denitrated; and then introducing the flue gas to be denitrated and the solid particles into the cloth bag reactor 2, wherein the solid particles are adsorbed on the surface of the cloth bag reactor 2 to react with the flue gas to be denitrated again, and the flue gas to be denitrated is converted into denitrated flue gas. The method comprises the steps of firstly enabling original flue gas and atomized supersaturated ammonium sulfite solution to flow in a spray drying tower 1 in parallel and contact with each other for reaction, drying the supersaturated ammonium sulfite solution into solid particles in the process of flow parallel and contact with each other, enabling the ammonium sulfite to react with nitric oxide in the original flue gas, enabling the denitrated flue gas and the solid particles to be introduced into a cloth bag reactor 2, enabling the solid particles to be adsorbed on the surface of the cloth bag reactor 2 to react with nitric oxide in the flue gas to be denitrated, and further improving the removal rate of denitration in the flue gas while separating generated ammonium sulfate.
Preferably, the temperature of the raw flue gas in the step 1 is 90-100 ℃, and the flow rate is 0.5-1m/s; the flow rate of the atomized supersaturated ammonium sulfite solution is 1-3m/s; in the step 2, the mass fraction of the urea solution is 30-40%, and the pH value of the generated solution containing ammonium sulfite is 6-7. The temperature of the original flue gas is regulated to 90-100 ℃, so that the supersaturated ammonium sulfite solution is convenient to evaporate into a solid state, and the desulfurization of the flue gas can be more complete by controlling the mass fraction of the urea solution and the pH value of the generated solution containing ammonium sulfite. The dosage ratio of the flue gas and the urea solution in the step 2 is limited by the pH value of the generated solution containing ammonium sulfite, so long as the pH value is 6-7 after the reaction is finished, the sulfur oxides in the flue gas can be completely reacted, in addition, a sulfur dioxide and nitrogen oxide analyzer is arranged on a flue IV of the system, the content of the purified sulfur and nitrate is analyzed, and if the content is unqualified, the circular purification is carried out again.
Example 2
On the basis of embodiment 1, the present embodiment relates to a system of a semi-dry treatment method for flue gas purification, as shown in fig. 1 to 5, including a spray drying tower 1 for making raw flue gas and atomized supersaturated ammonium sulfite solution in parallel flow contact with each other, a cloth bag reactor 2 for adsorbing solid particles and reacting ammonium sulfite in the solid particles with nitrogen oxide, a desulfurization absorption tower 4 for making denitrated flue gas and urea solution react, a concentration system 6 for evaporating and concentrating a generated liquid containing ammonium sulfite to obtain supersaturated ammonium sulfite solution, and a urea solution preparation device 5 for providing urea solution, wherein the bottom of the spray drying tower 1 is communicated with a flue i 7, the middle lower part of the spray drying tower 1 is communicated with the concentration system 6, the top of the spray drying tower 1 is communicated with the cloth bag reactor 2, the cloth bag reactor 2 is communicated with the middle lower part of the desulfurization absorption tower 4, the lower part of the desulfurization absorption tower 4 is communicated with the concentration system 6, and the urea solution preparation device 5 is communicated with the desulfurization absorption tower 4.
The system adopts a spray drying tower 1, supersaturated ammonium sulfite solution is sprayed in the spray drying tower 1, the supersaturated ammonium sulfite solution is atomized into fine liquid drops through a solution atomizer 102, the atomized fine liquid drops are rapidly evaporated in original flue gas to form small crystals, namely solid particles, and meanwhile, partial ammonium sulfite particles in the solid particles react with nitrogen oxides in the flue gas in the evaporation process to generate ammonium sulfate particles.
The spray drying tower 1 adopts gas-liquid parallel flow contact, the original flue gas and the atomized supersaturated ammonium sulfite solution flow upwards from the lower part of the spray drying tower 1, and the spray drying tower 1 has the basic requirements: ensuring sufficient contact time and area of gas and liquid; the gas phase and the liquid phase can be disturbed strongly, the operation range is wide, the operation is stable, and the resistance is small; has sufficient mechanical strength and corrosion resistance. The tower bottom is provided with a tower bottom swirler 101, and the raw flue gas generates rotation and centrifugal motion after passing through the tower bottom swirler 101, so that the gas and the liquid are fully contacted, and mass transfer reaction is carried out simultaneously. The solution atomizer 102 in the tower adopts a hollow cone pressure type atomizer, which is beneficial to the mass transfer reaction between hot flue gas and solution and the water evaporation of liquid drops. So that the solution is completely gasified and the solute is completely crystallized into powder or particles. Simultaneously controlling the flow velocity of flue gas in the tower to be 0.5-1m/s and the temperature to be 900-100 ℃. The diameter of the spray drying tower 1 is larger than the spray distance of the solution atomizer 102, and the nozzles can be arranged in a multilayer mode along the smoke direction according to the spray amount. The height of the spray drying tower 1 can ensure that the atomized supersaturated ammonium sulfite solution is completely gasified.
The system adopts a spray drying tower 1, and is shown in figures 1, 3-5: the spray drying tower 1 comprises a drying tower body 103, a tower bottom swirler 101 and a solution atomizer 102; a tower bottom cyclone 101 is arranged at the lower part in the cavity of the drying tower body 103, the drying tower body 103 positioned at the lower part of the tower bottom cyclone 101 is communicated with a flue I7, the drying tower body 103 positioned at the upper part of the tower bottom cyclone 101 is communicated with one end of a pipeline I12, one end of the pipeline I12 extends into the cavity of the drying tower body 103, a solution atomizer 102 is arranged, and the other end of the pipeline I12 is communicated with a concentration system 6; the top of the drying tower body 103 is communicated with the cloth bag reactor 2 through a flue II 8, the flue II 8 is communicated with one end of a bypass flue 9, a bypass valve 14 is arranged on the bypass flue 9, and the other end of the bypass flue 9 is communicated with a flue III 10.
The system adopts the cloth bag reactor 2, solid particles enter the cloth bag reactor 2 along with the flue gas, the solid particles are adsorbed on the surface of the cloth bag reactor 2, unreacted ammonium sulfite particles in the solid particles react with nitrogen oxides in the flue gas passing through the cloth bag reactor 2 again to generate ammonium sulfate particles, and when the pressure difference of the cloth bag reactor 2 is increased, the cloth bag reactor 2 is subjected to back flushing and discharging. The cloth bag reactor 2 is used for collecting dried solid particles, the solid particles are adsorbed on the surface of the cloth bag reactor 2, ammonium sulfite in the solid particles reacts with nitrogen oxide in flue gas passing through the cloth bag reactor 2, and ammonium sulfate particles are generated.
In order to completely separate solid particles, denitration in flue gas is more thorough, and influence on denitration of a system during reverse blowing of the cloth bag reactor 2 is reduced, the cloth bag reactor 2 is composed of a plurality of cloth bag units 201, the number of the set units is larger than 10, each cloth bag unit 201 is composed of a plurality of cloth bags 202, each unit inlet 203 is communicated, a unit outlet 207 is arranged at the top of each cloth bag unit 201, the unit outlets 207 are communicated with the middle lower part of the desulfurization absorption tower 4, the unit outlets 207 can be isolated independently and are used for mutual isolation during reverse blowing and operation of the cloth bag reactor 2, and a large-inclination-angle hopper 205 and a star-shaped valve 206 are arranged below each cloth bag unit 201 and are used for storing and discharging materials. The cloth bag reactor 2 is provided with a bypass flue 9, the bypass flue 9 is opened when the system is started, and the bypass flue 9 is closed when the temperature of the system rises. The cloth bag 202 is made of polyester or polypropylene fiber, so that the cloth bag 202 is prevented from being corroded by acid, can resist the temperature of 130 ℃, and has the characteristics of small water absorption and strong air permeability. The volume of the cloth bag reactor 2 is reduced by using a long cloth bag 202 with the diameter of 200-300mm and the length of 8-10m, and the filtering air speed of the cloth bag 202 is ensured to be 0.5-1m/min.
An outlet of each cloth bag unit 201 is provided with an air-operated valve 208, two adjacent cloth bag units 201 are provided with a communicating pipe 209 for back blowing outlets of the cloth bags 202, and the communicating pipe 209 is arranged at the lower port of the cloth bag unit 201. The bag 202 back-blowing fan 211 takes back-blowing air from the outlet of the induced draft fan 3, the back-blowing pressure is 2-3KPa, and the air quantity is controlled to be half of the running air quantity.
The system adopts a cloth bag reactor 2 which can be specifically as shown in figure 1-2: the cloth bag reactor 2 comprises at least 10 cloth bag units 201, the bottom of each cloth bag unit 201 is provided with a unit inlet 203, each unit inlet 203 is communicated with the top of the spray drying tower 1 through a flue II 8, the top of each cloth bag unit 201 is provided with a unit outlet 207, and each cloth bag unit 201 comprises at least 3 groups of communicated cloth bags 202. A communicating pipe 209 is arranged between the adjacent cloth bag units 201 and at the bottom of the cloth bag units 201, a back-blowing gas port 210 is arranged at the top of each cloth bag unit 201, the back-blowing gas port 210 is communicated with a back-blowing fan 211 through a back-blowing gas pipeline, a pneumatic valve 208 is arranged on the back-blowing gas pipeline at the back-blowing gas port 210, and another pneumatic valve 208 is arranged at the unit outlet 207. The bottom of each cloth bag unit 201 is hermetically provided with an inclined angle hopper 205, the bottom of each inclined angle hopper 205 is provided with a discharge outlet 204, and each discharge outlet 204 is provided with a star-shaped valve 206.
This system adopts desulfurization absorption tower 4, and the denitration flue gas through the denitration gets into desulfurization absorption tower 4 after carries out the desulfurization, and the desulfurization absorption liquid major component that generates is the mixed liquid of ammonium sulfite, contains the formation liquid of ammonium sulfite promptly, does not set up adsorption equipment in the desulfurization absorption tower 4, controls absorption liquid concentration and pH value 6-7, guarantees that desulfurization efficiency and ammonia escape are qualified.
The absorption tower adopts two items of countercurrent contact of gas-liquid, and the flue gas is from bottom to top, and the absorption solution flows from tower upper portion downwards to the liquid droplet form dispersion in the gaseous phase, and desulfurization absorption tower 4 should possess the basic requirement: ensuring sufficient contact time and area of gas and liquid; the gas phase and the liquid phase can be disturbed strongly, the operation range is wide, the operation is stable, and the resistance is small; has sufficient mechanical strength and corrosion resistance. The bottom links to each other with absorption tower circulating pump 402 and absorption tower play liquid pump 401, adopts the multilayer to spout in the desulfurization absorption tower 4, and the nozzle adopts pressure type toper nozzle, sprays that the angle is big, even and difficult the jam, sends the absorption liquid into nozzle department through the circulating pump. The demister 404 is arranged at the top of the tower, and the integrated tubular dust and mist removing demister 404 is adopted, so that liquid drop carrying is reduced, the content of sulfate in clean flue gas is reduced, and the demister 404 needs to be periodically washed by process water. The flow rate is adjusted by the urea delivery pump 502, and the pH value of the solution in the desulfurization absorption tower 4 is controlled to be 6-7.
The system adopts the desulfurization absorption tower 4, which can be specifically as shown in figure 1: the desulfurization absorption tower 4 comprises an absorption tower liquid outlet pump 401, an absorption tower circulating pump 402, a packing layer 403, a demister 404 and an absorption tower body 405, wherein an absorption tower liquid storage chamber 407 is arranged at the bottom of an inner cavity of the absorption tower body 405, the packing layer 403 and the demister 404 are sequentially arranged in the inner cavity of the absorption tower body 405 above the absorption tower liquid storage chamber 407 from bottom to top, the absorption tower body 405 located between the absorption tower liquid storage chamber 407 and the packing layer 403 is communicated with a cloth bag unit 201 through a flue III 10, the absorption tower liquid storage chamber 407 is communicated with one end of a circulating pipe I408, the other end of the circulating pipe I408 extends into the inner cavity of the absorption tower body 405 located between the packing layer 403 and the demister 404 and is provided with an absorption tower nozzle 406, the absorption tower circulating pump 402 is arranged on the circulating pipe I408, the top of the absorption tower body 405 is communicated with an IV flue 11, a sulfur dioxide and nitrogen oxide analyzer is arranged on the IV flue 11, and a pH meter is arranged in the absorption tower liquid storage chamber 407. And an induced draft fan 3 is arranged on the flue III 10, and the flue III 10 is communicated with a bypass flue 9.
The system adopts a desulfurization solution concentration system 6, and mainly comprises an evaporation liquid pump 601, an evaporation separator 602, an evaporation circulating pump 603, a steam heater 604, an evaporative condenser 605, a condensed water recovery tank 606, a water ring vacuum pump 607 and other devices. The desulfurization solution concentrating system 6 and its accessories should have corrosion resistance and sufficient mechanical strength, and the system uses low-pressure steam as a heat source to raise the temperature of the ammonium sulfite-containing product liquid by a steam separator. And introducing steam into the shell pass of the steam separator, performing indirect countercurrent heat exchange on the steam and the generated liquid containing ammonium sulfite from top to bottom, and finally condensing the steam into water to be discharged out of the steam separator. The condensed water enters the tube pass of the steam heater 604 through the evaporation circulating pump 603, and then enters the evaporation separator 602 to continuously and circularly heat the solution all the time.
The evaporative condenser 605 and the water ring vacuum pump 607 pump the interior of the evaporative separator 602 to negative pressure, thereby reducing the boiling point of the solution. When the device is operated, the condenser 605 is started to circulate cooling water, the circulating water enters the tube pass of the condenser 605, the steam enters the shell pass of the condenser 605, the two indirectly perform countercurrent heat exchange, the steam from the evaporation separator 602 is condensed into water, the water flows into the condensate water recovery tank 606 and is recycled, and the condensate water can be used for urea solution preparation and washing of the demister 404 of the desulfurization absorption tower 4. The temperature of the solution is controlled to be 70-80 ℃ again in the evaporation process of the desulfurization solution, the negative pressure is controlled to be 0.05-0.1MPa again, and the solid content is 2-10%. And (3) sending the generated liquid containing ammonium sulfite in the desulfurization absorption tower 4 into a concentration system 6 for concentration to enable the solution to reach a supersaturated state and the solid content to reach 2-10%. And then fed into the spray drying tower 1.
The desulfurization solution concentration system 6 adopted in the system can be specifically as shown in fig. 1: the concentration system 6 comprises an evaporation liquid outlet pump 601, an evaporation separator 602, an evaporation circulating pump 603, a steam heater 604, a condenser 605 and a water ring vacuum pump 607, wherein a tube pass inlet of the evaporation separator 602 is communicated with the liquid storage chamber 407 of the absorption tower through a pipeline II 13, the evaporation liquid outlet pump 601 is arranged on the pipeline II 13, a tube pass outlet on the side wall of the evaporation separator 602 is communicated with the drying tower body 103 through a pipeline I12, the evaporation liquid outlet pump 601 is arranged on the pipeline I12, a shell pass inlet of the evaporation separator 602 is connected with one end of a circulating pipe II 608, a shell pass outlet on the side wall of the bottom of the evaporation separator 602 is connected with the other end of the circulating pipe II 608, the evaporation circulating pump 603 and the steam heater 604 are sequentially arranged on the circulating pipe II 608 from the shell pass outlet to the shell pass inlet, a tube pass outlet on the top of the evaporation separator 602 is connected with a tube pass of the condenser 605 through an evaporation pipe 609, and a tube pass of the condenser 605 is further connected with the water ring vacuum pump 607.
The system also comprises a urea solution preparation device, as shown in fig. 1, the urea solution preparation device 5 mainly comprises a urea bin 503, a discharge star valve 206 weighing machine 504, a urea solution tank and stirrer 506 and a urea solution delivery pump 502. 30-40% of urea solution is prepared by adjusting the weighing machine 504 and the supplementary water amount. The urea liquid preparation device 5 comprises a liquid preparation tank 501, a delivery pump 502 and a delivery pipe 505, wherein the liquid preparation tank 501 is communicated with the absorption tower body 405 through the delivery pipe 505, and the delivery pipe 505 is provided with the delivery pump 502. The urea liquid preparation device 5 further comprises a urea bin 503, a stirrer 506 and a weighing machine 504, wherein the urea bin 503 is connected with the liquid preparation tank 501 through the weighing machine 504, and the stirrer 506 is arranged in the liquid preparation tank 501.
In addition, as shown in fig. 1, a sulfur dioxide and nitrogen oxide analyzer, a thermometer, a pressure gauge and an air gauge are sequentially installed on the flue I7, and a sulfur dioxide and nitrogen oxide analyzer, a thermometer, a pressure gauge and an air gauge are sequentially installed on the flue IV 11; a thermometer and a pressure gauge are arranged on the flue II 8 and the flue III 10 as required; a thermometer and a pH meter are arranged on the absorption tower liquid storage chamber 407, and a thermometer and a pH meter are arranged on the tube pass of the evaporation separator 602. Therefore, the temperature and the pressure of the operation of the whole system are convenient to monitor; install sulfur dioxide and nitrogen oxide analysis appearance through I7 in the flue and be convenient for detect the volume that contains the sulphur nitre of waiting to purify the flue gas, install sulfur dioxide and nitrogen oxide analysis appearance through IV 11 in the flue and be convenient for detect the volume that contains the sulphur nitre of purifying the back flue gas, be convenient for regulate and control the feeding volume of former flue gas.
The system of the semi-dry treatment method for flue gas purification of the embodiment works as follows:
(1) After the system is ready, 30-40% of urea solution is prepared in a urea solution preparation tank 501, the urea solution with a certain liquid level is fed into a desulfurization absorption tower 4, the liquid level is ensured to be circulated enough, and then an absorption tower circulating pump 402 is started to start absorption solution circulation;
(2) Starting the induced draft fan 3, inducing the original flue gas to carry out system temperature rise, opening a bypass valve 14 on a bypass flue 9 of the cloth bag reactor 2, simultaneously adjusting the air quantity and pressure of the system, and ensuring that the micro negative pressure in the spray drying tower 1 is-0.5-2 KPa and the flow rate is 0.5-1m/s. When the inlet temperature of the cloth bag reactor 2 reaches 130 ℃, the bypass valve 14 is closed, and the cloth bag reactor 2 is heated.
(3) When the pH value of the absorption liquid in the desulfurization absorption tower 4 is 6-7 and the temperature is 60-70 ℃, analyzing the concentration of the ammonium sulfite in the solution in the desulfurization absorption tower 4, and when the solution is close to saturation (the solubility is 60-70 g), starting an absorption tower liquid outlet pump 401 of the desulfurization absorption tower 4 to send the solution into the solution concentration system 6. Meanwhile, the urea solution is supplemented into the desulfurization absorption tower 4, and the normal desulfurization efficiency is kept. When the liquid level in the evaporation separator 602 reaches the middle part, the evaporation circulating pump 603 is started for circulation, the steam condenser 605 is filled with circulating water, the vacuum pump is started, and the negative pressure in the evaporation separator 602 is adjusted to be-0.05-0.1 Mpa. Then, steam is fed into the steam heater 604, and the solution is heated to evaporate and concentrate. When the solution in the evaporation separator 602 reaches a supersaturated state, the evaporation liquid pump 601 is started to send liquid into the spray dryer,
(4) Adjusting the mass of the solution sprayed into the spray drying tower 1, and controlling the temperature in the spray drying tower 1 to be between 90 and 100 ℃. And simultaneously, the feeding amount of the spray drying tower 1 is adjusted according to the concentration of nitrogen oxides in the clean flue gas at the outlet of the system.
(5) According to the pressure difference of the cloth bags 202 in the cloth bag reactor 2, when the pressure difference of the cloth bags 202 is 1.0-2.0KPa, a back flushing system of the cloth bag reactor 2 is started, each cloth bag unit 201 is subjected to back flushing in sequence, the pneumatic valve 208 at the outlet of the cloth bag unit 201 is closed during back flushing, the pneumatic valve 208 at the back flushing port 210 of the cloth bag unit 201 is opened, the back flushing fan 211 of the cloth bag reactor 2 is started, the back flushing time of each cloth bag unit 201 is determined to be 20-40s, after the back flushing of the cloth bag unit 201 is finished, the pneumatic valve 208 at the back flushing port 210 of the cloth bag unit 201 is closed, the back flushing valve 208 at the outlet of the cloth bag unit 201 is opened, the back flushing of the next cloth bag unit 201 is performed, the back flushing fan 211 is stopped after all the back flushing are finished, and the star-type valve 206 at the discharging outlet 204 is started for discharging.
To sum up, the utility model discloses a flue gas processing system can detach injurants such as sulfur dioxide and nitrogen oxide in former flue gas effectively, and the sulfur dioxide clearance reaches more than 99%, and the nitrogen oxide clearance is more than 80%, reduces the risk that the fume emission harmed the environment from this. Just the utility model discloses a flue gas processing system's simple structure, it is easy to make, uses safe and reliable, and the implementation of being convenient for is popularized and applied. The system can shorten the process, reduce the investment cost, utilize the desulfurization product to carry out the denitration reaction, the product ammonium sulfate does not need crystallization and filtration, can be used for other industrial raw materials, and no waste water is discharged, has practical application prospect.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", and the like, indicate the orientation or positional relationship indicated based on the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
In the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly, e.g., as being fixedly connected, detachably connected, or integrated; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be interconnected within two elements or in a relationship where two elements interact with each other unless otherwise specifically limited. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
Although embodiments of the present invention have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art without departing from the scope of the present invention.
Claims (10)
1. The system for the semi-dry method for purifying the flue gas is characterized by comprising a spray drying tower (1) for enabling raw flue gas and atomized supersaturated ammonium sulfite solution to be in parallel flow contact with each other, a cloth bag reactor (2) for adsorbing solid particles and enabling ammonium sulfite in the solid particles to react with nitrogen oxides, a desulfurization absorption tower (4) for enabling denitration flue gas and urea solution to react, a concentration system (6) for enabling generated liquid containing ammonium sulfite to be evaporated and concentrated to obtain supersaturated ammonium sulfite solution, and a urea solution preparation device (5) for providing the urea solution, wherein the bottom of the spray drying tower (1) is communicated with a flue I (7), the middle lower portion of the spray drying tower (1) is communicated with the concentration system (6), the top of the spray drying tower (1) is communicated with the cloth bag reactor (2), the cloth bag reactor (2) is communicated with the middle lower portion of the desulfurization absorption tower (4), the lower portion of the desulfurization absorption tower (4) is communicated with the concentration system (6), and the urea solution preparation device (5) is communicated with the desulfurization absorption tower (4).
2. The system for semidry method for flue gas purification according to claim 1, wherein the cloth bag reactor (2) comprises at least 10 cloth bag units (201), each cloth bag unit (201) is provided with a unit inlet (203) at the bottom, each unit inlet (203) is communicated with the top of the spray drying tower (1) through a flue II (8), each cloth bag unit (201) is provided with a unit outlet (207) at the top, and each cloth bag unit (201) comprises at least 3 groups of connected cloth bags (202).
3. Semi-dry process system for the purification of flue gases according to claim 2, characterized in that each of said cloth bags (202) is cylindrical with a diameter of 200-300mm and a length of 8-10m.
4. The semi-dry process system for flue gas purification according to claim 2, wherein a communicating pipe (209) is arranged between adjacent cloth bag units (201) and at the bottom of the cloth bag units (201), a back-blowing port (210) is arranged at the top of each cloth bag unit (201), the back-blowing port (210) is communicated with a back-blowing fan (211) through a back-blowing pipeline, a pneumatic valve (208) is arranged on the back-blowing pipeline at each back-blowing port (210), and another pneumatic valve (208) is arranged at the outlet (207) of the cloth bag units.
5. The semi-dry process system for flue gas purification according to claim 2, wherein the bottom of each cloth bag unit (201) is hermetically provided with a dip angle hopper (205), the bottom of each dip angle hopper (205) is provided with a discharge outlet (204), and a star-shaped valve (206) is arranged at each discharge outlet (204).
6. Semi-dry process system for flue gas cleaning according to claim 2, characterized in that the spray drying tower (1) comprises a drying tower body (103), a tower bottom cyclone (101) and a solution atomizer (102); a tower bottom cyclone (101) is arranged at the lower part in the cavity of the drying tower body (103), the drying tower body (103) positioned at the lower part of the tower bottom cyclone (101) is communicated with a flue I (7), the drying tower body (103) positioned at the upper part of the tower bottom cyclone (101) is communicated with one end of a pipeline I (12), one end of the pipeline I (12) extends into the cavity of the drying tower body (103), and one end of the pipeline I (12) is provided with a solution atomizer (102); the top of the drying tower body (103) is communicated with the cloth bag reactor (2) through a flue II (8), the flue II (8) is communicated with one end of a bypass flue (9), a bypass valve (14) is arranged on the bypass flue (9), and the other end of the bypass flue (9) is communicated with a flue III (10).
7. System of semi-dry process for flue gas cleaning according to claim 6, the desulfurization absorption tower (4) comprises an absorption tower liquid outlet pump (401), an absorption tower circulating pump (402), a packing layer (403), a demister (404) and an absorption tower body (405), an absorption tower liquid storage chamber (407) is arranged at the bottom of the inner cavity of the absorption tower body (405), a packing layer (403) and a demister (404) are sequentially arranged in the inner cavity of the absorption tower body (405) above the absorption tower liquid storage chamber (407) from bottom to top, the absorption tower body (405) between the absorption tower liquid storage chamber (407) and the packing layer (403) is communicated with the cloth bag unit (201) through a flue III (10), the liquid storage chamber (407) of the absorption tower is communicated with one end of a circulating pipe I (408), the other end of the circulating pipe I (408) extends into the inner cavity of the absorption tower body (405) between the filler layer (403) and the demister (404), and is provided with an absorption tower nozzle (406), an absorption tower circulating pump (402) is arranged on the circulating pipe I (408), the top of the absorption tower body (405) is communicated with a flue IV (11), and a sulfur dioxide and nitrogen oxide analyzer is arranged on the flue IV (11), and a pH meter is arranged in the absorption tower liquid storage chamber (407).
8. The semi-dry process system for flue gas purification according to claim 7, wherein an induced draft fan (3) is arranged on the flue III (10).
9. The system of the semi-dry method for flue gas purification according to claim 7, wherein the concentration system (6) comprises an evaporation liquid outlet pump (601), an evaporation separator (602), an evaporation circulating pump (603), a steam heater (604), a condenser (605) and a water ring vacuum pump (607), a tube side inlet of the evaporation separator (602) is communicated with the absorption tower liquid storage chamber (407) through a pipeline II (13), the evaporation liquid outlet pump (601) is arranged on the pipeline II (13), a tube side outlet on the side wall of the evaporation separator (602) is communicated with the drying tower body (103) through a pipeline I (12), the evaporation liquid outlet pump (601) is arranged on the pipeline I (12), a shell side inlet of the evaporation separator (602) is connected with one end of the circulating tube II (608), a shell side outlet on the bottom side wall of the evaporation separator (602) is connected with the other end of the circulating tube II (608), the evaporation liquid II (603) and the steam heater (605) are sequentially arranged on the circulating tube side outlet from the shell side outlet to the shell side inlet, and the condenser (605) is connected with the condenser (609) through the evaporation liquid outlet of the condenser (607) and the water ring vacuum pump (607).
10. The semi-dry method system for flue gas purification according to any one of claims 1 to 9, further comprising a urea liquid preparation device (5), wherein the urea liquid preparation device (5) comprises a liquid preparation tank (501), a delivery pump (502) and a delivery pipe (505), the liquid preparation tank (501) is communicated with the desulfurization absorption tower (4) through the delivery pipe (505), and the delivery pipe (505) is provided with the delivery pump (502).
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| CN115055034A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas purification |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115055034A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas purification |
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