CN115350500A - Byproduct comprehensive utilization system in foaming agent production - Google Patents
Byproduct comprehensive utilization system in foaming agent production Download PDFInfo
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- CN115350500A CN115350500A CN202211014908.9A CN202211014908A CN115350500A CN 115350500 A CN115350500 A CN 115350500A CN 202211014908 A CN202211014908 A CN 202211014908A CN 115350500 A CN115350500 A CN 115350500A
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- B01D53/34—Chemical or biological purification of waste gases
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- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
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- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
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Abstract
The utility model relates to a system is used multipurposely to accessory substance in foamer production, the separating unit is including consecutive first salt pond, crystallization separation module and first refrigerated centrifuge, the rectifying column links to each other with first salt pond, the liquid outlet of crystallization separation module links to each other with first refrigerated centrifuge, the refined unit is including consecutive second salt pond and edulcoration pond, the solid outlet of crystallization separation module links to each other with the second salt pond, the export of spray column links to each other with the edulcoration pond, and the edulcoration pond is connected with sodium chloride recovery pipeline. The chlorine-containing tail gas and the waste salt and alkali residues are recycled, so that the environmental pollution and the resource waste caused by direct discharge are avoided, the chlorine-containing tail gas is used for treating the waste salt and alkali residues (purified sodium chloride crude salt), the chlorine-containing tail gas and the waste salt and alkali residues are comprehensively treated, the treatment efficiency is improved, the utilization rate is high, the comprehensive utilization rate of the chlorine-containing tail gas and the waste salt and alkali residues is high, the treatment process is simple, and the sodium chloride and the sodium carbonate with high purity can be recycled.
Description
Technical Field
The application relates to the technical field of foaming agent production, in particular to a byproduct comprehensive utilization system in foaming agent production.
Background
The chemical foaming agent is azodicarbonamide, has the characteristics of stable property, large gas evolution, no pollution to products, no corrosion to molds and the like, and is the most widely applied chemical foaming agent at present. The foaming agent is widely applied to foaming of various thermoplastic plastics such as polyethylene, polyvinyl chloride, polypropylene, ethylene-vinyl acetate copolymer and the like, natural rubber, butyl rubber and the like. With diversification of the application field of foaming agent products and high-end product types, individual requirements of downstream manufacturers on product performance, technical service and the like of the foaming agent are continuously improved, and foaming agent production enterprises are required to have continuous innovation capability and can develop differentiated and applicable products according to customer requirements.
The method mainly adopts a urea method to produce the foaming agent, firstly adopts the working procedures of reacting urea and sodium hypochlorite in an alkaline solution to obtain hydrazine hydrate, refining the obtained hydrazine hydrate, carrying out a condensation reaction on the refined hydrazine hydrate and the urea in an acid environment to obtain an intermediate biurea, and finally carrying out an oxidation reaction on the biurea and chlorine to prepare the foaming agent. Specifically, in the biurea and chlorine gas oxidation reaction stage, an oxidation kettle is used as a carrier to perform oxidation reaction to generate a foaming agent, the oxidation kettle discharges tail gas in the working process, the tail gas mainly comprises chlorine gas and hydrogen chloride, resource waste can be caused if the tail gas is directly discharged, and the environment can be polluted, meanwhile, urea and sodium hypochlorite react in an alkaline solution to obtain hydrazine hydrate, a large amount of waste salt and alkali residues can be generated in the hydrazine hydrate production process by a urea method, and if the waste salt and alkali residues are not recycled, serious resource waste can be caused, and the environment can be polluted. It can be seen that chlorine-containing tail gas and waste salt and alkali residues are generated in the process of producing the foaming agent at present, and if the chlorine-containing tail gas and the waste salt and alkali residues are not recycled and directly discharged, the environment is polluted and the resource waste is also caused.
Disclosure of Invention
Therefore, in the process of producing the foaming agent by adopting the urea method in the prior art, in the oxidation reaction stage of biurea and chlorine, the oxidation kettle discharges chlorine-containing tail gas in the working process, a large amount of waste salt and alkali residues are generated in the process of producing hydrazine hydrate by adopting the urea method, if the chlorine-containing tail gas and the chlorine-containing tail gas are directly discharged without recycling, the environment is polluted, and resources are wasted. The comprehensive utilization system for byproducts in the production of the foaming agent is provided, the chlorine-containing tail gas and the waste salt and alkali residues are recycled, the environmental pollution and the resource waste caused by direct discharge are avoided, the chlorine-containing tail gas is used for treating the waste salt and alkali residues (purified sodium chloride crude salt) so that the chlorine-containing tail gas and the waste salt and alkali residues are comprehensively treated, the treatment efficiency and the utilization rate of the treatment system are higher, the comprehensive utilization rate of the chlorine-containing tail gas and the waste salt and alkali residues is high, the treatment process is simple, and the sodium chloride and the sodium carbonate with higher purity can be recycled.
The utility model provides a system is used multipurposely to accessory substance in foamer production, includes consecutive oxidation kettle and spray column and consecutive hydrazine reactor, rectifying column, separation unit and refined unit, the separation unit is including consecutive first salt pond, crystallization separation module and first freezing centrifuge, the rectifying column with first salt pond links to each other, the liquid outlet of crystallization separation module with first freezing centrifuge links to each other, refined unit is including consecutive second salt pond and edulcoration pond, the solid outlet of crystallization separation module with the second salt pond links to each other, the spray column has sodium hydroxide and sprays the liquid import, the export of spray column with the edulcoration pond links to each other, just the edulcoration pond is connected with sodium chloride recovery pipeline.
Preferably, in the above system for comprehensively utilizing byproducts in the production of foaming agents, a second refrigerated centrifuge is further included, the hydrazine reactor is connected to the second refrigerated centrifuge, and the second refrigerated centrifuge is connected to the rectifying tower.
Preferably, in the above system for comprehensively utilizing byproducts in production of foaming agents, the crystallization separation module includes a heating device and a centrifuge which are connected in sequence, the first salt pool is connected to the heating device, a liquid outlet of the centrifuge is connected to the first refrigerated centrifuge, and a solid outlet of the centrifuge is connected to the second salt pool.
Preferably, in the system for comprehensively utilizing byproducts in the production of foaming agents, the mother liquor outlet of the first refrigerated centrifuge is connected with the first salt pond.
Preferably, in the above system for comprehensive utilization of byproducts in production of foaming agents, the outlet of the spray tower is connected with the raw material inlet of the hydrazine reactor.
Preferably, in the comprehensive utilization system of byproducts in the production of foaming agents, the comprehensive utilization system further comprises an acidification tank, the impurity removal tank is connected with the acidification tank, and the acidification tank is connected with a hydrogen chloride introduction pipeline and a sodium chloride recovery pipeline.
Preferably, in the above byproduct comprehensive utilization system in the production of foaming agent, be provided with pH detection device in the acidizing pond, the hydrogen chloride lets in the pipeline and is provided with electronic flow valve, pH detection device with electronic flow valve electricity is connected.
Preferably, in the system for comprehensively utilizing byproducts in the production of foaming agents, electric stirring devices are arranged in the first salt pond and the second salt pond, and the first salt pond is provided with a preheating device.
Preferably, in the byproduct comprehensive utilization system in the production of the foaming agent, the hydrazine reactor is further connected with a tail gas recovery ammonia production system, the tail gas recovery ammonia production system comprises a cooler, a first condenser and a deamination tower, a tail gas outlet of the hydrazine reactor is connected with a tube pass inlet of the cooler, a gas phase outlet of the cooler is connected with a tube pass inlet of the first condenser, a liquid phase outlet of the cooler is a hydrazine hydrate recovery outlet, a tube pass outlet of the first condenser is connected with the deamination tower, the deamination tower is provided with an ammonia recovery pipeline, a shell pass inlet of the first condenser is a condensate water inlet, a shell pass outlet of the first condenser is communicated with a shell pass inlet of the cooler, a shell pass outlet of the cooler is a condensate water outlet, and the temperature of the condensate water entering the shell pass of the cooler is 40-80 ℃.
Preferably, in the comprehensive utilization system of byproducts in the production of foaming agents, the comprehensive utilization system further comprises a preheater, a tube side outlet of the first condenser is connected with a tube side inlet of the preheater, a tube side outlet of the preheater is connected with the deamination tower, a steam outlet of the hydrazine reactor is connected with a steam inlet of the deamination tower, and the ammonia recovery pipeline is connected with a shell side inlet of the preheater.
The technical scheme who this application adopted can reach following beneficial effect:
in the comprehensive utilization system of byproducts in the production of the foaming agent, waste salt and alkali residues discharged from the bottom of a rectifying tower are prepared into suspension in a first salt pond, solid-liquid separation is performed through a crystallization separation module, separated mother liquor is conveyed into a first freezing centrifuge, in the process of freezing separation of the mother liquor through the first freezing centrifuge, a large amount of sodium carbonate in the mother liquor is crystallized and separated, only a small amount of sodium chloride is crystallized and separated, the purity of a sodium carbonate product obtained by the process can reach 99%, crude sodium chloride salt separated by the crystallization separation module is introduced into a second salt pond and is dissolved in water to obtain crude sodium chloride, and then the crude sodium chloride is conveyed into an impurity removal pond, tail gas overflowing from an oxidation kettle is sprayed with tail gas through a sodium hydroxide solution to obtain sodium chloride and sodium hypochlorite, the treatment of chlorine-containing tail gas is completed, the sodium chloride and the sodium hypochlorite generated by spraying in the spraying tower are introduced into the impurity removal pond to be mixed with the crude sodium chloride in the impurity removal pond, and the crude sodium chloride solution has strong oxidizing property, so that impurities such as hydrazine hydrate, crude organic matters, sodium hypochlorite, crude sodium chloride and other impurities in the sodium chloride purification solution can be removed, and other ammonia nitrogen and the ammonia nitrogen chloride solution can be purified.
Therefore, the comprehensive utilization system for byproducts in the production of the foaming agent, disclosed by the application, recycles the chlorine-containing tail gas and the waste salt and alkali residues, avoids environmental pollution and resource waste caused by direct discharge, and the chlorine-containing tail gas is used for treating the waste salt and alkali residues (purified sodium chloride crude salt) so as to comprehensively treat the chlorine-containing tail gas and the waste salt and alkali residues, so that the treatment efficiency and the utilization rate of the treatment system are higher, the comprehensive utilization rate of the chlorine-containing tail gas and the waste salt and alkali residues is high, the treatment process is simple, and the sodium chloride and the sodium carbonate with higher purity can be recovered.
Drawings
FIG. 1 is a schematic diagram of a byproduct recycling system in the production of a blowing agent, disclosed in an embodiment of the present application.
Wherein: the system comprises an oxidation kettle 110, a spray tower 120, a hydrazine reactor 130, a rectifying tower 200, a separation unit 300, a first salt pond 310, a crystallization separation module 320, a heating device 321, a centrifuge 322, a first refrigerated centrifuge 330, a refining unit 400, a second salt pond 410, an impurity removal pond 420, a sodium chloride recovery pipeline 421, a second refrigerated centrifuge 500, an acidification pond 700 and a hydrogen chloride introduction pipeline 710.
Detailed Description
To facilitate an understanding of the present application, the present application will now be described more fully with reference to the accompanying drawings. Preferred embodiments of the present application are given in the accompanying drawings. This application may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.
It will be understood that when an element is referred to as being "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. As used herein, the terms "vertical," "horizontal," "left," "right," "top," "bottom," "top," and the like are for purposes of illustration only and do not represent the only embodiment.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein in the description of the present application is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.
Referring to fig. 1, an embodiment of the present application discloses a system for comprehensively utilizing byproducts in production of a foaming agent, which includes an oxidation kettle 110 and a spray tower 120 connected in sequence, and a hydrazine reactor 130, a rectification tower 200, a separation unit 300, and a refining unit 400 connected in sequence, that is, the oxidation kettle 110 and the spray tower 120 are connected in sequence, and the hydrazine reactor 130, the rectification tower 200, the separation unit 300, and the refining unit 400 are connected in sequence, wherein:
in the stage of obtaining hydrazine hydrate by reacting urea with sodium hypochlorite in an alkaline solution, the urea and the sodium hypochlorite react in a hydrazine reactor 130 to generate hydrazine hydrate and generate byproducts such as waste salt and alkali residues at the same time, therefore, the hydrazine hydrate discharged from the hydrazine reactor 130 contains a large amount of waste salt and alkali residues, the hydrazine reactor 130 is connected with a rectifying tower 200, so that a mixed solution of the hydrazine hydrate discharged from the hydrazine reactor 130 and the byproducts such as the waste salt and alkali residues is introduced into the rectifying tower 200, the hydrazine hydrate in the mixed solution is rectified and discharged from the top of the rectifying tower 200 in the rectifying tower 200, and the waste salt and alkali residues in the mixed solution are discharged from the bottom of the rectifying tower 200, thereby realizing the separation of the hydrazine hydrate and the waste salt and alkali residues in the mixed solution and finishing the rectification of the hydrazine hydrate. The working process and principle of rectifying hydrazine hydrate in the rectifying tower 200 are known technologies, and for the sake of brevity, detailed description is omitted here.
The waste salt and alkali residue discharged from the bottom of the rectifying tower 200 is introduced into a separation unit 300 for separating and recovering sodium carbonate and sodium chloride therein. Specifically, the separation unit 300 includes a first salt pond 310, a crystallization separation module 320, and a first refrigerated centrifuge 330, which are connected in sequence, the rectification tower 200 is connected to the first salt pond 310, the waste salt and alkali residue discharged from the bottom of the rectification tower 200 is introduced into the first salt pond 310, the waste salt and alkali residue is prepared into a suspension in the first salt pond 310, and a proper amount of hydrochloric acid can be added into the suspension to reduce the sodium hydroxide content in the suspension and meet the requirements of the subsequent processes. And then the suspension is introduced into a crystallization separation module 320 for solid-liquid separation, and sodium chloride crude salt and mother liquor in the suspension are separated. The liquid outlet of the crystallization separation module 320 is connected with the first freezing centrifuge 330, the separated mother liquor is conveyed into the first freezing centrifuge 330, the mother liquor is cooled by using chilled water, so that the solubility of sodium carbonate is reduced, sodium carbonate in the mother liquor is separated out, the separation is performed by the first freezing centrifuge 330, and as the solubility of other waste salt caustic sludge such as sodium chloride in water is not changed greatly along with the temperature and the sodium carbonate is sensitive to the temperature change, a large amount of sodium carbonate in the mother liquor is crystallized and separated in the process of freezing and separating the mother liquor by the first freezing centrifuge 330, only a small amount of sodium chloride is crystallized and separated, and the purity of the sodium carbonate product obtained by the process can reach 99%. The separated solid sodium carbonate can be conveyed to a soda plant to produce soda.
The crude salt of sodium chloride that the crystallization separation module 320 separated lets in to refine in the unit 400 and purify, refined unit 400 is including consecutive second salt pond 410 and edulcoration pond 420, the solid export of crystallization separation module 320 links to each other with second salt pond 410, the crude salt of sodium chloride that the crystallization separation module 320 separated lets in to second salt pond 410, add water and dissolve it and obtain the crude liquid of sodium chloride, then carry the crude liquid of sodium chloride after will dissolving to edulcoration pond 420. In the stage of oxidizing reaction of biurea and chlorine, the biurea and the chlorine are oxidized in the oxidation kettle 110 to generate biurea, meanwhile, tail gas continuously overflows from the oxidation kettle 110, the overflowing tail gas mainly comprises chlorine and hydrogen chloride, the tail gas is introduced into the spray tower 120, the spray tower 120 is provided with a sodium hydroxide spray liquid inlet, the tail gas is sprayed by a sodium hydroxide solution, and the tail gas reacts with the sodium hydroxide solution to generate sodium chloride and sodium hypochlorite, so that the treatment of the chlorine-containing tail gas is completed. The export of spray column 120 links to each other with edulcoration pond 420, it lets in edulcoration pond 420 with spraying the sodium chloride and the sodium hypochlorite that generate in the spray column 120, mix with the thick liquid of sodium chloride in the edulcoration pond 420, spray the sodium hypochlorite that generates in the spray column 120 and let in the thick liquid of sodium chloride, because sodium hypochlorite has strong oxidability, therefore, hydrazine hydrate in the thick liquid of sodium chloride can be detached to sodium hypochlorite, the organic matter, impurity such as ammonia nitrogen, purify with the thick liquid of sodium chloride, in order to detach other impurity in the thick liquid of sodium chloride, obtain the sodium chloride solution that the purity is higher, realize the purification of the thick salt of sodium chloride. The impurity removing tank 420 is connected with a sodium chloride recovery pipeline 421, then the sodium chloride solution with higher purity in the impurity removing tank 420 is recovered through the sodium chloride recovery pipeline 421, and then the sodium chloride solid with higher purity can be obtained through an evaporation crystallization mode.
In the comprehensive utilization system of byproducts in the production of foaming agents disclosed in the embodiment of the application, the mixed solution of byproducts such as hydrazine hydrate and waste salt and alkali residues discharged from a hydrazine reactor 130 is rectified by a rectifying tower 200 to obtain hydrazine hydrate with high purity, the waste salt and alkali residues discharged from the bottom of the rectifying tower 200 are prepared into suspension in a first salt pond 310, solid-liquid separation is performed by a crystallization separation module 320 to separate sodium chloride crude salt and mother liquor in the suspension, the separated mother liquor is conveyed into a first freezing centrifuge 330, the mother liquor is cooled by using chilled water, a large amount of sodium carbonate in the mother liquor is separated by crystallization in the process of freezing separation of the mother liquor by the first freezing centrifuge 330, only a small amount of sodium chloride is separated by crystallization, the purity of the sodium carbonate product obtained by the process can reach 99%, the sodium chloride crude salt separated by the crystallization separation module 320 is introduced into a second salt pond 410 to be dissolved by water to obtain sodium chloride crude liquor, then conveying the chlorine-containing tail gas to an impurity removal tank 420, simultaneously introducing the tail gas overflowing from the oxidation kettle 110 into a spray tower 120, spraying the tail gas through a sodium hydroxide solution to obtain sodium chloride and sodium hypochlorite, finishing the treatment of the chlorine-containing tail gas, introducing the sodium chloride and the sodium hypochlorite generated by spraying in the spray tower 120 into the impurity removal tank 420, mixing the sodium chloride and the sodium hypochlorite with the sodium chloride crude liquid in the impurity removal tank 420, and introducing the sodium hypochlorite generated by spraying in the spray tower 120 into the sodium chloride crude liquid.
Therefore, the comprehensive utilization system for byproducts in the production of the foaming agent, disclosed by the application, recycles the chlorine-containing tail gas and the waste salt and alkali residues, avoids environmental pollution and resource waste caused by direct discharge, and the chlorine-containing tail gas is used for treating the waste salt and alkali residues (purified sodium chloride crude salt) so as to comprehensively treat the chlorine-containing tail gas and the waste salt and alkali residues, so that the treatment efficiency and the utilization rate of the treatment system are higher, the comprehensive utilization rate of the chlorine-containing tail gas and the waste salt and alkali residues is high, the treatment process is simple, and the sodium chloride and the sodium carbonate with higher purity can be recovered.
Since only sodium carbonate in the mixed solution of hydrazine hydrate and waste salt and alkali residues discharged from the hydrazine reactor 130 is sensitive to temperature change, and the solubility of hydrazine hydrate, sodium chloride and other waste salt and alkali residues in water does not change greatly with the temperature, sodium carbonate can be directly recovered by freezing before rectification, in an optional embodiment, the system disclosed by the application can further comprise a second freezing centrifuge 500, the hydrazine reactor 130 is connected with the second freezing centrifuge 500, and the second freezing centrifuge 500 is connected with the rectification tower 200. Set up second refrigerated centrifuge 500 before rectifying column 200, directly freeze recovery sodium carbonate before the rectification, can reduce the volume of the useless salt caustic sludge that gets into rectifying column 200, under the less condition of volume of the useless salt caustic sludge that gets into rectifying column 200, rectifying column 200 is effectual to the rectification of hydrazine hydrate, the content of useless salt caustic sludge is still less in the hydrazine hydrate after the rectification, thereby can improve the rectification effect of rectifying column 200 to the hydrazine hydrate, simultaneously, through first refrigerated centrifuge 330 and the two-stage refrigerated separation sodium carbonate of second refrigerated centrifuge 500, can improve the rate of recovery of sodium carbonate.
As described above, the suspension is passed into the crystallization separation module 320 to perform solid-liquid separation, and sodium chloride crude salt and mother liquor in the suspension are separated, that is, the crystallization separation module 320 can separate the suspension into sodium chloride crude salt and mother liquor, in an alternative embodiment, the crystallization separation module 320 may include a heating device 321 and a centrifuge 322 connected in sequence, the first salt pool 310 is connected to the heating device 321, a liquid outlet of the centrifuge 322 is connected to the first refrigerated centrifuge 330, and a solid outlet of the centrifuge 322 is connected to the second salt pool 410. Firstly, the suspension is heated and evaporated by the heating device 321, the solubility of sodium carbonate is increased along with the increase of the temperature of the suspension, but the solubility of sodium chloride is kept unchanged, so that the sodium carbonate is completely dissolved under the heating and evaporation of the suspension by the heating device 321, only sodium chloride and other impurities are crystallized, then, solid-liquid separation is carried out by the centrifuge 322, and crude sodium chloride salt and mother liquor in which a large amount of sodium carbonate is dissolved are obtained by separation, so that the aim of separating the suspension into crude sodium chloride salt and the mother liquor is fulfilled, the separation effect is good, a large amount of sodium carbonate is prevented from being separated into the crude sodium chloride salt in the separation process, the purification of the crude sodium chloride salt is complicated, and the purity of the sodium carbonate separated by the first refrigerated centrifuge 330 can be ensured.
After first refrigerated centrifuge 330 separates the sodium carbonate, still contain the alkali sediment of waste salt in the mother liquor after the separation, the mother liquor export of first refrigerated centrifuge 330 links to each other with first salt pond 310, in letting in the mother liquor after the separation of first refrigerated centrifuge 330 in first salt pond 310, a waste salt alkali sediment for discharging at the bottom of the dissolving rectification tower 200 tower, and simultaneously, it can enter into the separation unit 300 again and separate to let in first salt pond 310, avoid direct emission, still contain the alkali sediment of waste salt in the mother liquor after the separation, direct emission still can cause environmental pollution and wasting of resources.
Preferably, the outlet of the spray tower 120 can be further connected to a raw material inlet of the hydrazine reactor 130, so that sodium hypochlorite generated by spraying in the spray tower 120 can be introduced into the hydrazine reactor 130 and used as a raw material of the hydrazine reactor 130, so that the spray tower 120 can provide a strong oxidant for the impurity removal tank 420 to purify the sodium chloride crude salt, and can also provide a production raw material (sodium hypochlorite) for the hydrazine reactor 130, thereby achieving the effect of multiple purposes and improving the practicability of the system. Specifically, the flow direction of the sodium hypochlorite generated by spraying in the spray tower 120 can be adjusted according to actual production needs, and the hydrazine reactor 130 or the impurity removal tank 420 is specifically introduced to be adjusted according to actual production needs.
Because the waste salt-alkali residue also contains a small amount of sodium hydroxide, and when sodium hypochlorite is input into the impurity removal tank 420 by the spray tower 120, the sodium hypochlorite generated by the spray tower 120 contains sodium hydroxide, the content of sodium hydroxide in the recovered sodium chloride is high, and the purity of the recovered sodium chloride is seriously influenced. Based on this, in an optional embodiment, the system disclosed in the present application may further include an acidification tank 700, the impurity removal tank 420 is connected to the acidification tank 700, and the acidification tank 700 is connected to a hydrogen chloride introduction pipe 710 and a sodium chloride recovery pipe 421. A proper amount of hydrochloric acid is added to the salt solution from which impurities have been removed in the acidification tank 700 to remove sodium hydroxide and sodium carbonate in the salt solution, and then sodium chloride is recovered through the sodium chloride recovery pipe 421, so that the purity of the recovered sodium chloride can be further improved.
Further, a pH detection device may be disposed in the acidification tank 700, the hydrogen chloride introduction pipe 710 is provided with an electric flow valve, and the pH detection device is electrically connected to the electric flow valve. The pH value of the salt solution is detected through the pH detection device, the amount of hydrochloric acid added into the acidification tank 700 can be controlled accurately, and the accuracy and controllability of the system disclosed by the application are improved.
Preferably, an electric stirring device may be provided in each of the first salt tank 310 and the second salt tank 410 to increase the salt dissolving speed and efficiency, and the first salt tank 310 is provided with a preheating device. To preheat the suspension formulated in the first salt bath 310, and may then be directly subjected to evaporative crystallization.
Urea and sodium hypochlorite react in the hydrazine reactor 130 to generate hydrazine hydrate, in order to perform heating reaction, the hydrazine reactor 130 needs to be heated by steam and heated to about 140 ℃, so that part of hydrazine and ammonia gas obtained by thermal decomposition of urea are discharged through a tail gas outlet, and the tail gas mainly contains hydrazine hydrate, ammonia and water vapor, and the hydrazine hydrate and the ammonia gas have different boiling points, so that the hydrazine hydrate and the ammonia gas can be condensed and recovered by utilizing the difference of the boiling points. The tail gas outlet of the hydrazine reactor 130 is connected with the tube pass inlet of the cooler, so that part of hydrazine hydrate and ammonia gas which are heated to become gas phases are introduced into the tube pass of the cooler for cooling, the temperature of condensed water entering the shell pass of the cooler is 40-80 ℃, namely the temperature of the condensed water in the shell pass of the cooler is 40-80 ℃, the boiling point of hydrazine hydrate is more than 40 ℃ and the boiling point of ammonia gas is less than 40 ℃, so that the cooler can condense the hydrazine hydrate in the tail gas into liquid, the liquid hydrazine hydrate is recovered through the liquid phase outlet of the cooler, namely the liquid phase outlet of the cooler is a hydrazine hydrate recovery outlet, ammonia water which is not condensed in the tail gas is discharged through the gas phase outlet of the cooler, the gas phase outlet of the cooler is connected with the tube pass inlet of the first condenser, the shell pass inlet of the first condenser is a condensed water inlet, so that the tail gas which is not condensed in the cooler is introduced into the tube pass of the first condenser and is continuously condensed through the condensed water in the shell pass of the first condenser to be condensed to be continuously condensed into the deamination tower, and ammonia gas is removed in a mixed solution in the deamination tower, and the mixed solution is extracted from the ammonia tower through an ammonia recovery tower. The working principle of ammonia gas removal from the mixed liquid by the deamination tower and the structure of the deamination tower are known technologies, and are not described herein for the sake of text brevity.
Because the condensed water in the cooler is at a temperature of 40-80 ℃, the temperature of the condensed water in the first condenser is higher than that of the condensed water in the first condenser, and a shell pass outlet of the first condenser is communicated with a shell pass inlet of the cooler, so that the condensed water after condensation heat exchange of the first condenser is introduced into a shell pass of the cooler, the temperature of the condensed water with the lower temperature is increased to above 40 ℃ after condensation heat exchange in the first condenser, and then the condensed water is introduced into the cooler to continuously condense the hydrazine hydrate in the tail gas, thereby realizing the cascade utilization of cold energy in the condensed water, avoiding energy waste, avoiding the additional supply of the condensed water with the temperature of 40-80 ℃ for the cooler, and saving the condensed water. The shell side outlet of the cooler is a condensed water outlet, so that the condensed water is recycled.
Above-mentioned technical scheme can realize the recovery of hydrazine hydrate and ammonia in the hydrazine hydrate production tail gas, avoids the wasting of resources, and can prevent that tail gas from directly discharging to the atmosphere to avoid causing environmental pollution problem. Meanwhile, condensed water after condensation heat exchange of the first condenser is introduced into a shell pass of the cooler, the temperature of the condensed water with lower temperature in the first condenser rises to more than 40 ℃ after condensation heat exchange, and then the condensed water is introduced into the cooler to continuously condense hydrazine hydrate in tail gas, so that cascade utilization of cold in the condensed water is realized, energy waste is avoided, the condensed water with the temperature of 40-80 ℃ can be prevented from being additionally provided for the cooler, and the condensed water can be saved.
The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.
The above-mentioned embodiments only express several embodiments of the present application, and the description thereof is more specific and detailed, but not construed as limiting the claims. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the concept of the present application, which falls within the scope of protection of the present application. Therefore, the protection scope of the present patent shall be subject to the appended claims.
Claims (10)
1. The utility model provides a by-product comprehensive utilization system in foamer production, characterized in that, including consecutive oxidation kettle (110) and spray column (120) and consecutive hydrazine reactor (130), rectifying column (200), separating unit (300) and refined unit (400), separating unit (300) are including consecutive first salt pond (310), crystallization separation module (320) and first refrigerated centrifuge (330), rectifying column (200) with first salt pond (310) links to each other, the liquid outlet of crystallization separation module (320) with first refrigerated centrifuge (330) links to each other, refined unit (400) are including consecutive second salt pond (410) and edulcoration pond (420), the solid outlet of crystallization separation module (320) with second salt pond (410) link to each other, spray column (120) have sodium hydroxide spray liquid import, the export of spray column (120) with edulcoration pond (420) link to each other, and edulcoration pond (420) are connected with sodium chloride recovery pipeline (421).
2. The system for recycling byproducts in the production of foaming agent as claimed in claim 1, further comprising a second refrigerated centrifuge (500), wherein said hydrazine reactor (130) is connected to said second refrigerated centrifuge (500), and said second refrigerated centrifuge (500) is connected to said rectifying tower (200).
3. The system for comprehensively utilizing byproducts in the production of foaming agents, as claimed in claim 1, wherein the crystallization separation module (320) comprises a heating device (321) and a centrifuge (322) which are connected in sequence, the first salt pond (310) is connected with the heating device (321), a liquid outlet of the centrifuge (322) is connected with the first freezing centrifuge (330), and a solid outlet of the centrifuge (322) is connected with the second salt pond (410).
4. The system for recycling byproducts in the production of foaming agent as claimed in claim 1, wherein the mother liquor outlet of said first refrigerated centrifuge (330) is connected to said first salt pond (310).
5. The system for recycling byproducts in the production of foaming agent as claimed in claim 1, wherein the outlet of said spray tower (120) is connected to the raw material inlet of said hydrazine reactor (130).
6. The system for comprehensively utilizing the byproducts in the production of the foaming agent as claimed in claim 1, further comprising an acidification tank (700), wherein the impurity removal tank (420) is connected with the acidification tank (700), and the acidification tank (700) is connected with a hydrogen chloride introduction pipeline (710) and the sodium chloride recovery pipeline (421).
7. The system for comprehensively utilizing the byproducts generated in the production of the foaming agent as claimed in claim 1, wherein a pH detection device is arranged in the acidification tank (700), the hydrogen chloride inlet pipeline (710) is provided with an electric flow valve, and the pH detection device is electrically connected with the electric flow valve.
8. The system for comprehensively utilizing the byproducts in the production of the foaming agent as claimed in claim 1, wherein an electric stirring device is arranged in each of the first salt pond (310) and the second salt pond (410), and the first salt pond (310) is provided with a preheating device.
9. The system for comprehensively utilizing byproducts in foaming agent production as claimed in claim 1, wherein the hydrazine reactor (130) is further connected with a tail gas recovery ammonia production system, the tail gas recovery ammonia production system comprises a cooler, a first condenser and a deamination tower, a tail gas outlet of the hydrazine reactor is connected with a tube side inlet of the cooler, a gas phase outlet of the cooler is connected with a tube side inlet of the first condenser, a liquid phase outlet of the cooler is a hydrazine hydrate recovery outlet, a tube side outlet of the first condenser is connected with the deamination tower, the deamination tower is provided with an ammonia recovery pipeline, a shell side inlet of the first condenser is a condensate water inlet, a shell side outlet of the first condenser is communicated with a shell side inlet of the cooler, a shell side outlet of the cooler is a condensate water outlet, and the temperature of the condensate water entering the shell of the cooler is 40 ℃ to 80 ℃.
10. The system of claim 9, further comprising a preheater, wherein the tube side outlet of the first condenser is connected to the tube side inlet of the preheater, the tube side outlet of the preheater is connected to the deamination tower, the vapor outlet of the hydrazine reactor is connected to the vapor inlet of the deamination tower, and the ammonia recovery conduit is connected to the shell side inlet of the preheater.
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