CN216172385U - Production system of ternary hydrotalcite for desorption nitrogen oxide - Google Patents
Production system of ternary hydrotalcite for desorption nitrogen oxide Download PDFInfo
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Abstract
The utility model discloses a production system of ternary hydrotalcite, in particular to a production system of ternary hydrotalcite for removing nitrogen oxides, which comprises the following components: the device comprises a trimetal salt preparation kettle and a carbonized ammonia water solution preparation kettle, wherein the lower outlet of the trimetal salt preparation kettle is connected with the inlet of a high-speed reactor through a pipeline, the lower outlet of the carbonized ammonia water solution preparation kettle is connected with the inlet of the high-speed reactor through a pipeline, the outlet of the high-speed reactor is connected with the inlet of an aging tank through a pipeline, and the outlet of the aging tank is connected with the inlet of a plate-and-frame filter press through a pipeline. The production system of desorption ternary hydrotalcite for nitrogen oxide that this application provided is rational in infrastructure, and production efficiency is high, excellent in use effect.
Description
Technical Field
The utility model relates to the technical field of chemical equipment, relates to a production system of ternary hydrotalcite, and particularly relates to a production system of ternary hydrotalcite for removing nitrogen oxides.
Background
Nitrogen-containing tail gas is often discharged in many industrial fields, such as tail gas generated in industrial production of coal-fired thermoelectricity, refining, cement and the like and tail gas discharged by automobiles contain nitrogen oxides, particularly the discharge of NO and other nitrogen oxides can cause harm, and atmospheric pollution brings difficulty to environmental protection. The nitrogen oxide in the atmosphere reacts with hydrocarbon through ultraviolet irradiation to form toxic smog, the photochemical smog has special smell, stimulates eyes, damages plants and can reduce atmospheric visibility, and the nitrogen oxide stimulates lungs, thus being easy to cause respiratory diseases.
Nitrogen oxides are one of the main pollution sources causing atmospheric pollution, and there are several kinds of nitrogen oxides NOx: comprising N20、NO、N02、N2O3、N2O4And N2O5Etc., wherein NO and N02Is a main component, under the condition of high-temperature combustion, NOx mainly exists in the form of NO, and NO in the initially discharged NOx accounts for about 95%, so that denitration mainly removes NO.
From the viewpoint of NO structure, two main methods for removing NO are used, namely control in the combustion process to directly convert NO into NO2And can be removed by absorption or the like, which is a method controlled from a source. The other is removal after combustion, which is divided into dry and wet removal of NO. The wet removal process has simple equipment requirement and low operation temperature, but has limited industrial application due to complex system and higher cost. The dry method has the advantages that all operations are carried out at high temperature, no wastewater is generated, the generated flue gas does not need to be heated again, the denitrification efficiency is higher, and the method is particularly applied in large-scale industrial production in a large scale. Among them, dry denitrification is divided into selective catalytic reduction and selective non-catalytic reduction. The selective non-catalytic reduction method is to reduce NOx by using a reducing agent under the condition of high temperature, does not use a catalyst, but has high reaction temperature and reductionThe dosage of the agent is large, mainly the NOx reduction rate is only 50-60%, the effect is not ideal, and secondary pollution is easy to cause. The selective catalytic reduction method has the advantages that different catalysts are used, the reduction rate can be higher, secondary pollution cannot be caused, but the method has the obvious defects that most of the catalysts depend on import, the price is relatively expensive, the catalysts are easy to poison and lose efficacy in use, and the like, so that the selective catalytic reduction method is used for replacing domestic denitration catalysts, reducing the use of precious metals and heavy metals, realizing large-scale production and reducing the cost, and is beneficial to post-treatment and regeneration of the catalysts, and therefore, the method has important practical significance in batch production of high-efficiency denitration catalysts.
The catalytic reduction method is a method in which NOx is reduced to N by a reducing agent (ammonia, hydrogen, carbon monoxide, etc.) under the action of a catalyst2And H2O。
The method can realize the removal of NOx at different temperatures, and the removal efficiency can reach 70-90%, and can reach more than 90% under excellent conditions.
In order to reduce the emission of nitrogen oxides, extensive research has been carried out in various countries for many years, and the methods mainly used for denitration by catalytic reduction, denitration by non-catalytic reduction, denitration by adsorption, denitration by electron beam and the like. In reality, the components and the contents of the discharged tail gas of each device are different, and the adopted denitration methods are also different. Catalytic reduction denitration is still adopted in more in refining and other chemical industries, and is widely adopted due to good denitration effect, but the catalyst is usually imported from abroad, and the imported denitration agent usually contains precious metals, is expensive, has too high use cost and brings difficulty to wide use, so that a domestic denitration agent is urgently needed to be produced, the transportation cost is reduced, the price is low, the subsequent treatment is convenient, the cost is low, and the wide popularization is convenient.
Numerous attempts have been made at removing nitrogen oxides at home and abroad, and some available methods have been obtained, such as a method for removing nitrogen oxides by adsorption and plasma selective catalytic reduction provided by the patent with the application number of 201110062090.3, wherein the adsorption catalyst is any one of hydrotalcite, hydrotalcite-like compound, natural zeolite, synthetic zeolite or activated alumina modified by hydrogen ions or metal ions; chenhongying and the like research the good NO removal of the cobalt-containing hydrotalcite oxide by using a CO reducing agent; the Xiamei and the like also carry out denitration research on the nickel-aluminum-cerium ternary hydrotalcite as a catalyst, and the method verifies that the hydrotalcite can be used as a denitration catalyst, has good effect and is worthy of popularization.
The denitration effect of the catalysts is good, but only a laboratory synthesis method is provided, and a complete set of process equipment is needed to meet the requirement of mass production in the process of converting the catalysts into large-scale industrial production, so that the production process for producing the high-efficiency denitration catalyst is designed to meet the requirement of mass production from practical consideration, comprehensive production and application problems, and the social requirement is met.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the problems in the prior art, and provides a production system of ternary hydrotalcite for removing nitrogen oxides, so as to solve the technical problems at present.
The technical scheme adopted by the utility model for solving the technical problems is as follows:
the utility model provides a production system of ternary hydrotalcite for removing nitrogen oxides, which comprises the following components: the device comprises a trimetal salt preparation kettle and a carbonized ammonia water solution preparation kettle, wherein the lower outlet of the trimetal salt preparation kettle is connected with the inlet of a high-speed reactor through a pipeline, the lower outlet of the carbonized ammonia water solution preparation kettle is connected with the inlet of the high-speed reactor through a pipeline, the outlet of the high-speed reactor is connected with the inlet of an aging tank through a pipeline, and the outlet of the aging tank is connected with the inlet of a plate-and-frame filter press through a pipeline.
Preferably, a filtrate outlet of the plate-and-frame filter press is respectively connected with a mother liquor tank and a washing water tank through pipeline valves, a mother liquor outlet of the mother liquor tank is connected with a mother liquor discharge pipeline through a pipeline connected with a material pump and a valve in series, an inlet of the washing water tank is connected with a washing water outlet of the plate-and-frame filter press through a pipeline valve, and an outlet of the washing water tank is connected with a washing water inlet of the plate-and-frame filter press through a pipeline connected with a material pump and a valve in series.
Preferably, the washing water inlet of the plate-and-frame filter press is also connected with a purified water pipeline.
Preferably, the lower filter cake outlet of the plate-and-frame filter press is respectively connected with the pulping tank and the material inlet of the belt conveyor through pipeline valves.
Preferably, the upper inlet of the beating tank is simultaneously connected with the lower filter cake outlet of the plate-and-frame filter press and a purified water pipeline, and the outlet of the beating tank and the material outlet of the aging tank are connected with the inlet of the plate-and-frame filter press through pipelines which are connected with a material pump in series.
Preferably, a material pump between the pulping tank and the plate-and-frame filter press and a pipeline between the plate-and-frame filter press are connected with a crystallization kettle in parallel, and a jacket of the crystallization kettle is connected with a steam pipeline.
Preferably, the feed opening of the belt conveyor is connected with a material inlet of the flash dryer through a pipeline, a lower air inlet of the flash dryer is connected with a hot air pipeline, an upper outlet of the flash dryer is connected with an upper inlet of a first cyclone separator through a pipeline, an upper outlet of the first cyclone separator is connected with an upper inlet of a first bag-type dust collector through a pipeline, an upper air outlet of the first bag-type dust collector is connected with an inlet of an exhaust fan through a pipeline valve, and an outlet of the exhaust fan is connected with a pipeline for exhausting air outwards; and the lower discharge ports of the first bag-type dust collector and the first cyclone separator are connected with the feed port of the auger conveyor.
Preferably, the discharge port of the auger conveyor is connected with the feed port of the scintillation boiling calciner through a pipeline, the feed port of the scintillation boiling calciner is simultaneously connected with the outlet pipeline of the heater through a pipeline, and the inlet of the heater is connected with the blower through a pipeline.
Preferably, an upper outlet of the scintillation boiling calciner is connected with an inlet of a gas-gas heat exchanger through a pipeline, an outlet of the gas-gas heat exchanger is connected with an inlet of a second cyclone separator through a pipeline, and a shell pass lower inlet and a shell pass upper outlet of the gas-gas heat exchanger are respectively connected with a cold air inlet and a hot air outlet.
Preferably, the upper air outlet of the second cyclone separator is connected with the upper inlet of the second bag-type dust collector through a pipeline, the upper air outlet of the second bag-type dust collector is connected with the inlet of the exhaust fan through a pipeline valve, the outlet of the exhaust fan is connected with a pipeline for exhausting air outwards, and the lower discharge ports of the second cyclone separator and the second bag-type dust collector are connected with a packaging system for calcined hydrotalcite.
The utility model has the beneficial effects that: the utility model provides a series of production processes of preparation, reaction, aging, filtering, washing, drying, molding, calcining and the like of ternary hydrotalcite for removing nitrogen oxides, wherein the production processes comprise production equipment, processes and the like.
Drawings
The above aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a schematic diagram of a system for producing ternary hydrotalcite for removing nitrogen oxides according to an embodiment of the present invention.
Description of reference numerals:
in FIG. 1, 1-trimetallic salt preparation vessel; 2-carbonized ammonia water preparation tank; 3-a first cyclone separator; 4-a first bag-type dust collector; 5-high speed reactor; 6-an aging tank; 7-plate and frame filter press; 8, a pulping tank; 9-washing water tank; 10-mother liquor tank; 11-a belt conveyor; 12-flash dryer; 13-a second cyclone separator; 14-a second bag-type dust collector; 16-auger conveyor; 17-a blower; 18-a heater; 19-scintillation boiling calciner; 20-gas heat exchanger; 21-crystallization kettle.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The utility model provides a production system of ternary hydrotalcite for removing nitrogen oxides, which comprises the following components: the device comprises a trimetal salt preparation kettle 1 and a carbonized ammonia water solution preparation kettle 2, wherein the upper feed inlet of the trimetal salt preparation kettle 1 is respectively connected with aqueous solutions of nickel salt, aluminum salt and cerium salt and a purified water pipeline, and the lower outlet of the trimetal salt preparation kettle is connected with the inlet of a high-speed reactor 5 through a pipeline which is connected with a material pump and a flowmeter in series; the inlet and outlet of the jacket of the trimetal salt preparation kettle 1 are respectively connected with the inlet and outlet of a high-temperature steam pipeline, the upper feed inlet of the carbonized ammonia water solution preparation kettle 2 is respectively connected with ammonium bicarbonate, ammonia water and a pure water pipeline, and the lower outlet is connected with the inlet of the high-speed reactor 5 through a pipeline which is connected with a material pump and a flowmeter in series; the outlet of the high-speed reactor 5 is connected with the inlet of the aging tank 6 through a pipeline, and the outlet of the aging tank 6 is connected with the inlet of the plate-and-frame filter press 7 through a pipeline which is connected with a material pump and a valve in series; a filtrate outlet of the plate-and-frame filter press 7 is respectively connected with a mother liquor tank 10 and a washing water tank 9 through pipeline valves; a mother liquor outlet of the mother liquor tank 10 is connected with a mother liquor discharge pipeline through a pipeline which is connected with a material pump and a valve in series; the inlet of the water washing tank 9 is respectively connected with the water washing outlet of the plate-and-frame filter press 7 through a pipeline valve; the outlet of the water washing tank 9 is connected with a washing water inlet and an outward discharge pipeline of the plate-and-frame filter press 7 through a pipeline which is connected with a material pump and a valve in series; a washing water inlet of the plate-and-frame filter press 7 is simultaneously connected with a purified water pipeline through which purified water circulates inside; the lower filter cake outlet of the plate-and-frame filter press 7 is respectively connected with the material feeding holes of the pulping tank 8 and the belt conveyor 11 through pipeline valves; an upper inlet of the pulping tank 8 is simultaneously connected with a lower filter cake outlet of the plate-and-frame filter press 7 and a purified water pipeline, and an outlet of the pulping tank 8 and a material outlet of the aging tank 6 are connected with an inlet of the plate-and-frame filter press through pipelines which are connected with material pumps in series; a material pump between the pulping tank 8 and the plate-and-frame filter press 7 and a pipeline between the plate-and-frame filter press 7 are connected in parallel with a crystallization kettle 21, and a jacket of the crystallization kettle 21 is connected with a steam pipeline in which steam circulates.
A feed opening of the belt conveyor 11 is connected with a material inlet of the flash dryer 12 through a pipeline, a lower air inlet of the flash dryer 12 is connected with a hot air pipeline, and an upper outlet of the flash dryer 12 is connected with an upper inlet of the first cyclone separator 3 through a pipeline; an upper outlet of the first cyclone separator 3 is connected with an upper inlet of the first bag-type dust collector 4 through a pipeline; an air outlet at the upper part of the first bag-type dust collector 14 is connected with an inlet of an exhaust fan through a pipeline valve, and an outlet of the exhaust fan is connected with a pipeline for exhausting air outwards; the lower discharge ports of the first bag-type dust collector 4 and the first cyclone separator 3 are connected with the feed port of the auger conveyor 16; the discharge hole of the auger conveyor 16 is connected with the feed hole of the scintillation boiling calciner 19 through a pipeline; the feed inlet of the scintillation boiling calciner 19 is simultaneously connected with the outlet pipeline of the heater 18 through a pipeline, and the inlet of the heater 18 is connected with the blower 17 through a pipeline; the upper outlet of the scintillation boiling calciner 19 is connected with the inlet of a gas-gas heat exchanger 20 through a pipeline; an outlet of the gas-gas heat exchanger 20 is connected with an inlet of the second cyclone separator 13 through a pipeline, and a shell pass lower inlet and a shell pass upper outlet of the gas-gas heat exchanger 20 are respectively connected with a cold air inlet and a hot air outlet; an upper air outlet of the second cyclone separator 13 is connected with an upper inlet of a second bag-type dust collector 14 through a pipeline, an upper air outlet of the second bag-type dust collector 14 is connected with an inlet of an exhaust fan through a pipeline valve, and an outlet of the exhaust fan is connected with a pipeline for exhausting air outwards; the discharge ports at the lower parts of the second cyclone separator 13 and the second bag-type dust collector 14 are connected with a packaging system of calcined hydrotalcite.
The three-metal salt preparation kettle and the carbonized ammonia water preparation tank can adopt reaction kettles which are common in the market, a high-speed reactor, an aging tank, a plate-and-frame filter press, a belt conveyor, a pulping tank, a flash evaporation dryer, a first cyclone separator, a first bag-type dust collector, a second cyclone separator, a second bag-type dust collector, a packing auger conveyor, a blower, an exhaust fan, a heater, a flash boiling calciner and a crystallization kettle adopt equipment which is common in the market, and a gas-gas heat exchanger is a heat exchanger for exchanging heat between two gases; the water washing tank and the mother liquor tank are both common storage tanks.
The method for producing the hydrotalcite for denitration catalyst by using the ternary hydrotalcite production system comprises the following steps:
adding solid soluble tri-salt solution (nickel, cobalt, copper salt, aluminum, cerium salt, etc.) into tri-metal salt preparation kettle 1, adding a certain amount of pure water, heating and stirring at 70-100 deg.C, and adding M2+/M3+＝2～2.2：1，M2+Is a divalent metal ion, and is a metal ion,M3+is the sum of trivalent metal ions, wherein Ce3+/Al3+0.1-0.8, and preparing a mixed salt solution of three salts; mixing ammonia water, ammonium bicarbonate and pure water in a carbonized ammonia water preparation tank 2 to prepare a carbonized ammonia water buffer solution with mixed ammonia-salt concentration of 5-10%; the two solutions are sent into a high-speed reactor 5 through a material pump by a flowmeter, the reaction temperature is controlled to be 50-90 ℃, the rotating speed of a stirrer of the high-speed reactor 5 is 400-1000 rpm, the reaction lasts for 30-40 minutes, the reacted materials enter an aging device 6, the aging is carried out for 12-24 hours at the temperature of 80-100 ℃, hydrotalcite crystals are generated, then the materials are sent into a plate-and-frame filter press 7 through the material pump, the materials are filtered and washed for many times until the materials are qualified, and the filtrate enters a mother liquor tank 10 and then is sent to a subsequent processing device through the material pump for processing; the washing water is provided by a washing water tank 9 and is recycled or discharged. And (3) feeding the qualified hydrotalcite into a pulping tank 8, pumping the pulped slurry into a crystallization kettle 21 through a material pump, keeping the slurry at the temperature of 120-180 ℃ for 2-10 hours for crystal form reforming, and conveying the reformed material to a plate-and-frame filter press from the self pressure.
In order to improve the washing efficiency, the filter cake after each filter pressing is washed to the pulping tank 8 by water, and is pumped to a filter press for filter pressing by a material pump after the pulping tank 8 is fully washed; and finally, conveying the materials which are washed and filter-pressed to a flash evaporation dryer 12 by using a belt conveyor 11 or a flood dragon conveyor for flash evaporation drying, conveying wet materials to a bottom feed inlet of the flash evaporation dryer 12 by using a screw feeder, performing heat convection with hot air conveyed to the flash evaporation dryer, smashing and drying the materials by a stirrer and hot air driven by a motor at the bottom, conveying the dried materials to a first cyclone separator 3 along with the hot air, separating the materials, and discharging tail gas from a system by using a draught fan after the tail gas enters a first bag-type dust collector 4 to further collect the materials. The dried hydrotalcite is conveyed to a bottom feeding pipeline of a scintillation boiling calciner by an auger conveyor 16, is brought into the calciner by hot air fed by a heater 18, enters a heat exchanger 20 for cold air heat exchange and cooling after a calcined hydrotalcite framework at 500-700 ℃, namely mixed metal oxide of tri-salt, enters a second cyclone separator 13 and a second bag-type dust collector 14, is collected after calcination, and is exhausted by an induced draft fan.
And removing the denitration agent preparation section from the calcined hydrotalcite skeleton or the tri-salt composite oxide to form catalyst particles. According to different application sites and different components of the tail body containing the nitrate, the denitration catalyst with the required granularity, shape, aperture and specific surface area meeting the requirements can be directly prepared for denitration, or an adhesive, a reducing agent, a pore-forming agent, a synergist and the like are added to prepare the required denitration agent.
Example 1:
preparing Ni-Al-Ce ternary hydrotalcite by the above process, and using M2+/M3+＝2～2.2，Ce3+/Al3+Under the conditions that the temperature is 0.2-0.5 and the PH value is 5.3-5.9, the Ni-Al-Ce ternary composite metal oxide obtained by calcining at 500-700 ℃ is used as a catalyst, part of adhesive, synergist, pore-forming agent and the like are added, a granulator is used for preparing 40-60-mesh particles, the particles are calcined for 3-4 hours at 300-400 ℃ under the protection of nitrogen, the particles of the denitrifying agent are prepared, and H is used for preparing the denitrifying agent particles2As a reducing agent, when the concentration of NO is 250-500 ppm, the NO removal rate reaches 90-95% at 450 ℃.
Example 2:
preparing Cu-Al-Ce ternary hydrotalcite by the above process, and using M2+/M3+＝2～2.2，Ce3+/Al3+Calcining the Cu-Al-Ce ternary composite metal oxide catalyst at 500-700 ℃ under the conditions that the pH value is 0.2-0.5 and the pH value is 5.0-6.2, adding part of adhesive, synergist, pore-forming agent and the like, preparing particles of 40-60 meshes by using a granulator, calcining the particles for 3-4 hours at 300-400 ℃ under the protection of nitrogen, preparing particles of a denitration agent, and preparing particles of the denitration agent by using NH3As a reducing agent, when the concentration of NO is 250-500 ppm, the NO removal rate reaches 88-94% at 420 ℃.
Example 3:
preparing Co-Al-Ce ternary hydrotalcite by the above process, using M2+/M3+＝2～2.2，Ce3+/Al3+Under the conditions that the temperature is 0.2-0.5 and the PH value is 8.0-10.0, calcining at 500-700 ℃ to obtain Co-Al-Ce ternary composite metal oxide serving as a catalyst, adding part of adhesive, synergist, pore-forming agent and the like, preparing into 40-60-mesh particles by using a granulator, calcining at 300-400 ℃ for 3-4 hours under the protection of nitrogen, and preparing the denitration agent particlesCO is used as a reducing agent, and when the concentration of NO is 250-500 ppm, the NO removal rate reaches 91-94% at 100-300 ℃.
Example 4:
preparing Ni-Al-Ce-ternary hydrotalcite by the above process, and using M2+/M3+＝2～2.2，Ce3+/Al3+The method comprises the following steps of calcining at 500-700 ℃ under the conditions that 0.2-0.5 is achieved, and the PH value is 5.3-5.9 to obtain the Ni-Al-Ce ternary composite metal oxide catalyst, adding part of ammonium bicarbonate, adhesive, synergist, pore-forming agent and the like, preparing into 40-60-mesh particles by using a granulator, calcining for 3-4 hours at 300-400 ℃ under the protection of nitrogen to prepare denitration agent particles, using ammonium bicarbonate in the denitration agent as a reducing agent, and enabling the NO removal rate to reach 88-92% at 100-300 ℃ when the NO concentration is 250-500 ppm.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the utility model.
Claims (9)
1. A production system of ternary hydrotalcite for removing nitrogen oxides comprises: the kettle is prepared to trimetal salt and carbonization aqueous ammonia solution, its characterized in that: the lower outlet of the trimetal salt preparation kettle is connected with the inlet of the high-speed reactor through a pipeline, the lower outlet of the carbonized ammonia water solution preparation kettle is connected with the inlet of the high-speed reactor through a pipeline, the outlet of the high-speed reactor is connected with the inlet of an aging tank through a pipeline, and the outlet of the aging tank is connected with the inlet of a plate-and-frame filter press through a pipeline.
2. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 1, characterized in that: the filter liquor outlet of the plate-and-frame filter press is respectively connected with a mother liquor tank and a washing water tank through pipeline valves, the mother liquor outlet of the mother liquor tank is connected with an outer-discharging pipeline of mother liquor through pipelines which are connected with a material pump and a valve in series, the inlet of the washing water tank is respectively connected with the washing water outlet of the plate-and-frame filter press through pipeline valves, the outlet of the washing water tank is connected with the washing water inlet and an outer-discharging pipeline of the plate-and-frame filter press through pipelines which are connected with the material pump and the valve in series, and the washing water inlet of the plate-and-frame filter press is simultaneously connected with a pure water pipeline.
3. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 1, characterized in that: and the lower filter cake outlet of the plate-and-frame filter press is respectively connected with the pulping tank and the material feeding port of the belt conveyor through pipeline valves.
4. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 3, characterized in that: the upper inlet of the pulping tank is simultaneously connected with the lower filter cake outlet of the plate-and-frame filter press and a purified water pipeline, and the outlet of the pulping tank and the material outlet of the aging tank are connected with the inlet of the plate-and-frame filter press through pipelines which are connected with material pumps in series.
5. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 4, characterized in that: and a material pump between the pulping tank and the plate-and-frame filter press and a pipeline between the plate-and-frame filter press are connected with a crystallization kettle in parallel, and a jacket of the crystallization kettle is connected with a steam pipeline.
6. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 3, characterized in that: the feed opening of band conveyer passes through the material import of pipe connection flash dryer, the hot air line of lower part air intake connection of flash dryer, the upper portion export of flash dryer passes through the upper portion import of the first cyclone of pipe connection, the upper portion export of first cyclone passes through the upper portion import of the first sack cleaner of pipe connection, the import of line valve connection air exhauster is passed through to the upper portion air outlet of first sack cleaner, the pipeline of externally airing exhaust of exit linkage of air exhauster, the feed inlet of auger conveyer is connected to the lower part discharge gate of first sack cleaner and first cyclone.
7. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 6, characterized in that: the discharge port of the auger conveyor is connected with the feed port of the scintillation boiling calciner through a pipeline, the feed port of the scintillation boiling calciner is simultaneously connected with the outlet pipeline of the heater through a pipeline, and the inlet of the heater is connected with the air blower through a pipeline.
8. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 7, characterized in that: the upper outlet of the scintillation boiling calciner is connected with the inlet of a gas-gas heat exchanger through a pipeline, the outlet of the gas-gas heat exchanger is connected with the inlet of a second cyclone separator through a pipeline, and the shell side lower inlet and the shell side upper outlet of the gas-gas heat exchanger are respectively connected with a cold air inlet and a hot air outlet.
9. The system for producing ternary hydrotalcite for removing nitrogen oxides according to claim 8, characterized in that: the upper air outlet of the second cyclone separator is connected with the upper inlet of the second bag-type dust collector through a pipeline, the upper air outlet of the second bag-type dust collector is connected with the inlet of the exhaust fan through a pipeline valve, the outlet of the exhaust fan is connected with an external exhaust pipeline, and the lower discharge ports of the second cyclone separator and the second bag-type dust collector are connected with a calcined hydrotalcite packaging system.
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| CN115253666A (en) * | 2022-07-04 | 2022-11-01 | 江苏理工学院 | Method for removing VOCs (volatile organic compounds) by coupling hydrotalcite-like compound with low-temperature plasma and application |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115253666A (en) * | 2022-07-04 | 2022-11-01 | 江苏理工学院 | Method for removing VOCs (volatile organic compounds) by coupling hydrotalcite-like compound with low-temperature plasma and application |
| CN115253666B (en) * | 2022-07-04 | 2023-05-30 | 江苏理工学院 | Method for removing VOCs by hydrotalcite-like coupling low-temperature plasma and application |
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