CN204265470U - Ammonium chloride evaporation and crystallization system - Google Patents

Ammonium chloride evaporation and crystallization system Download PDF

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Publication number
CN204265470U
CN204265470U CN201420725932.8U CN201420725932U CN204265470U CN 204265470 U CN204265470 U CN 204265470U CN 201420725932 U CN201420725932 U CN 201420725932U CN 204265470 U CN204265470 U CN 204265470U
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CN
China
Prior art keywords
interchanger
heat exchanger
pipeline
tank
cooling
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
CN201420725932.8U
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Chinese (zh)
Inventor
蔡卫宜
谭兆基
黄家力
姚卫全
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
QINGYUAN ZHONGYU ENVIRONMENTAL PROTECTION INDUSTRIAL Co Ltd
Original Assignee
QINGYUAN ZHONGYU ENVIRONMENTAL PROTECTION INDUSTRIAL Co Ltd
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Filing date
Publication date
Application filed by QINGYUAN ZHONGYU ENVIRONMENTAL PROTECTION INDUSTRIAL Co Ltd filed Critical QINGYUAN ZHONGYU ENVIRONMENTAL PROTECTION INDUSTRIAL Co Ltd
Priority to CN201420725932.8U priority Critical patent/CN204265470U/en
Application granted granted Critical
Publication of CN204265470U publication Critical patent/CN204265470U/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

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Abstract

The utility model discloses ammonium chloride evaporation and crystallization system, comprise primary heater unit, evaporation unit and crystallization apparatus, primary heater unit comprises the temperature regulating tank, fresh feed pump, the First Heat Exchanger that connect successively with pipeline, the condensation-water drain of First Heat Exchanger is connected with cooling tank through pipeline, the tank skin of temperature regulating tank is pasted with circulating water channel, and cooling tank is connected with cooling tank with piping loop; Evaporation unit comprises vapour generator, the second interchanger and separator, the discharge end of First Heat Exchanger is connected with the feed end of the second interchanger, the condensation-water drain of the second interchanger is connected with cooling tank, and the steam-in of First Heat Exchanger, the second interchanger is all connected with vapour generator with pipeline; Crystallization apparatus comprises cooling crystallizer and negative pressure generator, and the discharge end of separator is connected with the feed end of cooling crystallizer, and the outlet of negative pressure generator is connected with the entrance of cooling crystallizer.The utility model energy efficiency utilization steam also reclaims the energy of water of condensation, and energy consumption is low.

Description

Ammonium chloride evaporation and crystallization system
Technical field
The utility model relates to ammonium chloride evaporation and crystallization system.
Background technology
Ammonium chloride is comparatively large in trade effluent toxic, can havoc ecotope, therefore, generally the trade effluent of ammonium chloride need be had to carry out the art breading of evaporative crystallization to me.But at present for the equipment of this art breading, need consume the device for generation of cold air or heat such as many quantity of steams or electric energy, cause technique consumes resources more, energy consumption is high, and cost is also very high.
Utility model content
In order to overcome the deficiencies in the prior art, the purpose of this utility model is to provide ammonium chloride evaporation and crystallization system, can efficiency utilization steam reclaim the energy of water of condensation, and energy consumption is low.
The purpose of this utility model adopts following technical scheme to realize:
Ammonium chloride evaporation and crystallization system, comprise primary heater unit, evaporation unit and crystallization apparatus, primary heater unit comprises the temperature regulating tank, fresh feed pump, the First Heat Exchanger for preheating that connect successively with pipeline, the condensation-water drain of First Heat Exchanger is connected with cooling tank through pipeline, the tank skin of temperature regulating tank is pasted with circulating water channel, cooling tank connects this circulating water channel with piping loop, and pipeline is connected with the first forced circulation pump between cooling tank and circulating water channel;
Evaporation unit comprises vapour generator, the second interchanger and separator, the discharge end of First Heat Exchanger is connected with the feed end of the second interchanger, the condensation-water drain of the second interchanger is connected with cooling tank, the steam-in of First Heat Exchanger, the second interchanger is all connected with vapour generator with pipeline, the discharge end of the second interchanger is connected with separator through one second forced circulation pump, and the vapour outlet of separator is also connected with vapour generator;
Crystallization apparatus comprises cooling crystallizer and negative pressure generator, and the discharge end of separator is connected with the feed end of cooling crystallizer, and the outlet of negative pressure generator is connected with the entrance of cooling crystallizer.
Preferably, the pipeline of described first forced circulation pump exit end is connected with reverse checkvalve.
Preferably, the pipeline between the steam-in of described First Heat Exchanger and vapour generator is connected with throttling valve.
Compared to existing technology, the beneficial effects of the utility model are:
The utility model is by the pump circulation of the first forced circulation pump, the water of condensation being flowed into cooling tank by First Heat Exchanger and the second interchanger can be delivered to circulating water channel, and for regulating the temperature of circulating water channel, make the temperature near room temperature in temperature regulating tank, be beneficial to the buffering of trade effluent, cold filtration and follow-up heating; Simultaneously, the steam that vapour generator produces can supply First Heat Exchanger, the second interchanger simultaneously, make the two obtain steam supply simultaneously, reduce the own loss that vapour generator stores up steam, and under the pump function of the second forced circulation pump, make separator, the second interchanger formation closed cycle, with efficiency utilization steam, in conjunction with the recycling of water of condensation, greatly to reduce energy consumption, reduce cost.
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail.
Accompanying drawing explanation
Fig. 1 is the connection diagram of the utility model ammonium chloride evaporation and crystallization system.
In figure: 1, temperature regulating tank; 2, fresh feed pump; 3, First Heat Exchanger; 4, cooling tank; 5, circulating water channel; 6, the first forced circulation pump; 7, vapour generator; 8, the second interchanger; 9, separator; 10, the second forced circulation pump; 11, cooling crystallizer; 12, negative pressure generator; 13, reverse checkvalve; 14, throttling valve.
Embodiment
Ammonium chloride evaporation and crystallization system as shown in Figure 1, comprise primary heater unit, evaporation unit and crystallization apparatus, primary heater unit comprises the temperature regulating tank 1, fresh feed pump 2, the First Heat Exchanger 3 for preheating that connect successively with pipeline, the condensation-water drain of First Heat Exchanger 3 is connected with cooling tank 4 through pipeline, the tank skin of temperature regulating tank 1 is pasted with circulating water channel 5, cooling tank 4 connects this circulating water channel 5 with piping loop, and pipeline is connected with the first forced circulation pump 6 between cooling tank 4 and circulating water channel 5;
Evaporation unit comprises vapour generator 7, second interchanger 8 and separator 9, the discharge end of First Heat Exchanger 3 is connected with the feed end of the second interchanger 8, the condensation-water drain of the second interchanger 8 is connected with cooling tank 4, the steam-in of First Heat Exchanger 3, second interchanger 8 is all connected with vapour generator 7 with pipeline, the discharge end of the second interchanger 8 is connected with separator 9 through one second forced circulation pump 10, and the vapour outlet of separator 9 is also connected with vapour generator 7;
Crystallization apparatus comprises cooling crystallizer 11 and negative pressure generator 12, and the discharge end of separator 9 is connected with the feed end of cooling crystallizer 11, and the outlet of negative pressure generator 12 is connected with the entrance of cooling crystallizer 11.
By the pump circulation of the first forced circulation pump 6, the water of condensation being flowed into cooling tank 4 by First Heat Exchanger 3 and the second interchanger 8 can be delivered to circulating water channel 5, and for regulating the temperature of circulating water channel 5, and then the temperature near room temperature making in temperature regulating tank 1, be beneficial to the buffering of trade effluent, cold filtration and follow-up heating; Simultaneously, the steam that vapour generator 7 produces can supply First Heat Exchanger 3, second interchanger 8 simultaneously, make the two obtain steam supply simultaneously, reduce the own loss that vapour generator 7 stores up steam, and under the pump function of the second forced circulation pump 10, make separator 9, second interchanger 8 form closed cycle, with efficiency utilization steam, in conjunction with the recycling of water of condensation, greatly to reduce energy consumption, reduce cost.
Particularly, external industrial waste water is introduced into temperature regulating tank 1, to regulate the water temperature of trade effluent, and impurity is precipitated, filters and cushions.By the effect of cooling tank 4 and the first forced circulation pump 6, the water of condensation of First Heat Exchanger 3 and the second interchanger 8 and circulating water channel 5 is made to realize the water cycle of mobility, for the temperature of trade effluent is adjusted to room temperature.Trade effluent enters First Heat Exchanger 3 under the pump function of fresh feed pump 2, and with First Heat Exchanger 3 heat exchange and ascending temperature, obtain pre-heat effect, the heat of this heat exchange is provided by vapour generator 7.Waste water after preheating accesses the second interchanger 8, a large amount of heat energy is obtained at the second interchanger 8, this a large amount of heat energy proposes 7 confessions by vapour generator, and the waste water with comparatively high temps enters separator 9 and realizes flash distillation, separation, forms steam and discharges and loop back vapour generator 7, form concentrated solution simultaneously, this concentrated solution enters cooling crystallizer 11, under the suction function of negative pressure generator 12, is able to drying, and realize crystallization, form ammonia chloride crystal.
As preferred embodiment, the pipeline of the first forced circulation pump 6 exit end is connected with reverse checkvalve 13, to prevent the aqueous reflux of circulating water channel 5 from returning cooling tank 4, is beneficial to the water temperature of controlled circulation tank 5.
As preferred embodiment, pipeline between the steam-in of described First Heat Exchanger 3 and vapour generator 7 is connected with throttling valve 14, this throttling valve 14 can limit the quantity of steam towards First Heat Exchanger 3, to control the quantity of steam provided First Heat Exchanger 3, realizes effective preheating.
Certainly, discharging pump can be added at the concentrated solution outlet of separator 9, accelerate to make concentrated solution to enter cooling crystallizer 11, and the negative pressure that in fact negative pressure generator 12 produces enter cooling crystallizer 11 automatically to be enough to allow concentrated solution pressurized.
Above-mentioned embodiment is only preferred implementation of the present utility model; can not limit the scope of the utility model protection with this, change and the replacement of any unsubstantiality that those skilled in the art does on basis of the present utility model all belong to the utility model scope required for protection.

Claims (3)

1. ammonium chloride evaporation and crystallization system, it is characterized in that: comprise primary heater unit, evaporation unit and crystallization apparatus, primary heater unit comprises the temperature regulating tank, fresh feed pump, the First Heat Exchanger for preheating that connect successively with pipeline, the condensation-water drain of First Heat Exchanger is connected with cooling tank through pipeline, the tank skin of temperature regulating tank is pasted with circulating water channel, cooling tank is connected with cooling tank with piping loop, and pipeline is connected with the first forced circulation pump between cooling tank and circulating water channel;
Evaporation unit comprises vapour generator, the second interchanger and separator, the discharge end of First Heat Exchanger is connected with the feed end of the second interchanger, the condensation-water drain of the second interchanger is connected with cooling tank, the steam-in of First Heat Exchanger, the second interchanger is all connected with vapour generator with pipeline, the discharge end of the second interchanger is connected with separator through one second forced circulation pump, and the vapour outlet of separator is also connected with vapour generator;
Crystallization apparatus comprises cooling crystallizer and negative pressure generator, and the discharge end of separator is connected with the feed end of cooling crystallizer, and the outlet of negative pressure generator is connected with the entrance of cooling crystallizer.
2. ammonium chloride evaporation and crystallization system according to claim 1, is characterized in that: the pipeline of described first forced circulation pump exit end is connected with reverse checkvalve.
3. ammonium chloride evaporation and crystallization system according to claim 1 and 2, is characterized in that: the pipeline between the steam-in of described First Heat Exchanger and vapour generator is connected with throttling valve.
CN201420725932.8U 2014-11-26 2014-11-26 Ammonium chloride evaporation and crystallization system Expired - Fee Related CN204265470U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201420725932.8U CN204265470U (en) 2014-11-26 2014-11-26 Ammonium chloride evaporation and crystallization system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201420725932.8U CN204265470U (en) 2014-11-26 2014-11-26 Ammonium chloride evaporation and crystallization system

Publications (1)

Publication Number Publication Date
CN204265470U true CN204265470U (en) 2015-04-15

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CN201420725932.8U Expired - Fee Related CN204265470U (en) 2014-11-26 2014-11-26 Ammonium chloride evaporation and crystallization system

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106698561A (en) * 2016-12-29 2017-05-24 哈尔滨工程大学 Device for treating biurea condensation sewage generated from preparation of ADC (Azodicarbonamide) foaming agent with urea method and use method of device

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106698561A (en) * 2016-12-29 2017-05-24 哈尔滨工程大学 Device for treating biurea condensation sewage generated from preparation of ADC (Azodicarbonamide) foaming agent with urea method and use method of device
CN106698561B (en) * 2016-12-29 2019-05-21 哈尔滨工程大学 A kind of urea method preparation ADC foaming agent biruea condensation sewage-treatment plant and its application method

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C14 Grant of patent or utility model
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20150415

Termination date: 20191126

CF01 Termination of patent right due to non-payment of annual fee