CN220002966U - Liquid alkali evaporation concentration system - Google Patents
Liquid alkali evaporation concentration system Download PDFInfo
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- CN220002966U CN220002966U CN202321542459.5U CN202321542459U CN220002966U CN 220002966 U CN220002966 U CN 220002966U CN 202321542459 U CN202321542459 U CN 202321542459U CN 220002966 U CN220002966 U CN 220002966U
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- evaporator
- heat exchanger
- liquid alkali
- liquid
- plate heat
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- 239000007788 liquid Substances 0.000 title claims abstract description 186
- 239000003513 alkali Substances 0.000 title claims abstract description 160
- 238000001704 evaporation Methods 0.000 title claims abstract description 34
- 230000008020 evaporation Effects 0.000 title claims abstract description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 63
- 238000010438 heat treatment Methods 0.000 claims description 30
- 239000003518 caustics Substances 0.000 claims description 29
- 238000003860 storage Methods 0.000 claims description 24
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 239000000463 material Substances 0.000 claims description 5
- 239000011552 falling film Substances 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 abstract description 11
- 230000007547 defect Effects 0.000 abstract description 3
- 239000012141 concentrate Substances 0.000 description 10
- 238000000034 method Methods 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 230000005494 condensation Effects 0.000 description 5
- 238000009833 condensation Methods 0.000 description 5
- 238000005868 electrolysis reaction Methods 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical class [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Abstract
The utility model provides a liquid alkali evaporation concentration system, which takes high-temperature high-pressure raw steam supplied by a steam pipeline as an initial heat source to carry out evaporation concentration on liquid alkali in a third evaporator; the steam generated after the concentration of the liquid alkali in the third evaporator is used as a heat source in the second evaporator to carry out evaporation concentration on the liquid alkali in the second evaporator; the system of the utility model overcomes the defect that steam and energy are wasted due to the fact that the liquid alkali is concentrated to be close to a saturated state in the traditional concentrated liquid alkali mode by the aid of the cooperation of the equipment.
Description
Technical Field
The utility model relates to the technical field of evaporation concentration, in particular to a liquid alkali evaporation concentration system.
Background
The chlor-alkali industry refers to the industry of preparing sodium hydroxide (NaOH), chlorine (Cl 2) and hydrogen (H2) by electrolysis of saturated sodium chloride solutions and producing a series of chemical products from them. In production, the concentration of the liquid alkali output from the electrolysis section is low, only 32% wt, and it is difficult to directly use it for producing flake alkali, so that it is required to concentrate it to a nearly saturated state (the concentration of the saturated aqueous sodium hydroxide solution is 52% wt) before it can be used for producing flake alkali.
In the prior art, some liquid alkali with the concentration of 32%wt is directly heated to be close to a saturated state by steam, but the mode has extremely high energy consumption and wastes steam; therefore, some enterprises adopt a two-stage countercurrent evaporation concentration method, namely, firstly, the liquid alkali with the concentration of 32 percent by weight is evaporated and concentrated to an intermediate concentration, and then the liquid alkali with the intermediate concentration is concentrated to be close to a saturated state by utilizing the recycled steam, so that compared with the method of directly concentrating the liquid alkali with the low concentration to be close to the saturated state, the method has the advantages that the consumed steam and energy are reduced, but the energy is still not fully utilized.
Disclosure of Invention
The utility model provides a liquid alkali evaporation concentration system which is used for solving the problem that the steam energy cannot be fully utilized in the existing concentrated liquid alkali mode.
The utility model provides a liquid alkali evaporation concentration system, which comprises a liquid alkali pipeline and a steam pipeline;
the liquid alkali pipeline is sequentially connected with a first evaporator, a first liquid alkali pump, a second evaporator, a second liquid alkali pump, a third evaporator, a third liquid alkali pump, a first plate heat exchanger and a finished product alkali storage tank in series;
a second plate heat exchanger is arranged between the first liquid alkali pump and the second evaporator;
a first tubular heat exchanger is arranged between the second liquid alkali pump and the third evaporator, the second liquid alkali pump is connected with a tube side inlet of the first tubular heat exchanger, and a tube side outlet of the first tubular heat exchanger is connected with a material inlet of the third evaporator;
the third liquid caustic pump is connected with a shell side inlet of the first tubular heat exchanger; the shell side outlet of the first tubular heat exchanger is connected with the heating medium inlet of the second plate heat exchanger, and the heating medium outlet of the second plate heat exchanger is connected with the first plate heat exchanger;
the steam pipeline is connected with the third evaporator, the second evaporator, the first evaporator and the surface condenser in series.
Optionally, the system of the utility model further comprises a third plate heat exchanger and a second tube heat exchanger;
the third plate heat exchanger and the second plate heat exchanger are connected with the first liquid alkali pump and the second evaporator in a parallel mode;
the second tubular heat exchanger and the first tubular heat exchanger are connected with the second liquid caustic pump and the third evaporator in a parallel mode.
Optionally, the system of the present utility model further comprises a condensate storage tank, and the first evaporator, the second evaporator, the third evaporator and the surface condenser are all connected to the condensate storage tank.
Optionally, the condensate outlet of the third evaporator is connected with the shell side inlet of the second tubular heat exchanger; the shell side outlet of the second tubular heat exchanger is connected with the heating medium inlet of the third plate heat exchanger.
Optionally, a first gas-blocking drain tank is arranged between the second evaporator and the condensate storage tank;
a second gas-blocking water drain tank is arranged between the third evaporator and the second tubular heat exchanger.
Optionally, the first plate heat exchanger is one of a flat plate heat exchanger, a hot plate heat exchanger or a spiral plate heat exchanger.
Optionally, the first evaporator, the second evaporator and the third evaporator are falling film evaporators.
The system of the utility model takes high-temperature high-pressure raw steam supplied by a steam pipeline as an initial heat source to evaporate and concentrate liquid alkali in a third evaporator; the steam generated after the concentration of the liquid alkali in the third evaporator is used as a heat source in the second evaporator to carry out evaporation concentration on the liquid alkali in the second evaporator; the system uses the equipment to evaporate and concentrate the low-concentration liquid alkali at room temperature step by step to obtain high-concentration liquid alkali meeting the standard, and can fully utilize the steam heat energy after the liquid alkali is evaporated, so that the system has the beneficial effects of fully utilizing the steam heat, saving the steam use amount and saving the energy sources, and overcomes the defect that the steam energy caused by concentrating the liquid alkali to be close to the saturated state cannot be fully utilized in the traditional concentrated liquid alkali mode.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions of the prior art, the following description will briefly explain the drawings used in the embodiments or the description of the prior art, and it is obvious that the drawings in the following description are some embodiments of the present utility model, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a liquid caustic soda evaporation concentration system according to an embodiment of the present utility model;
FIG. 2 is a schematic diagram of a liquid caustic soda evaporation concentration system according to another embodiment of the present utility model;
FIG. 3 is a schematic illustration of a liquid caustic evaporation concentration system according to yet another embodiment of the present utility model;
fig. 4 is a schematic diagram of a liquid caustic soda evaporation and concentration system according to another embodiment of the present utility model.
Reference numerals illustrate:
1. a liquid caustic line; 2. a first evaporator; 3. a second evaporator; 4. a third evaporator; 5. a finished product alkali storage tank; 6. a steam line; 7. a surface condenser; 8. a condensate storage tank; 21. a first liquid caustic pump; 22. a second plate heat exchanger; 23. a third plate heat exchanger; 24. a first gas-blocking water drain tank; 31. a second liquid caustic pump; 32. a first tubular heat exchanger; 33. a second tubular heat exchanger; 34. a second gas-blocking water drain tank; 41. a third liquid caustic pump; 42. a first plate heat exchanger.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present utility model more clear, the technical solutions in the embodiments of the present utility model will be clearly and completely described below, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are also within the scope of the utility model.
As shown in fig. 1, the utility model provides a liquid alkali evaporation concentration system, which comprises a liquid alkali pipeline 1 and a steam pipeline 6;
the liquid caustic pipeline 1 is sequentially connected with a first evaporator 2, a first liquid caustic pump 21, a second evaporator 3, a second liquid caustic pump 31, a third evaporator 4, a third liquid caustic pump 41, a first plate heat exchanger 42 and a finished caustic storage tank 5 in series;
a second plate heat exchanger 22 is arranged between the first liquid caustic pump 21 and the second evaporator 3;
a first tubular heat exchanger 32 is arranged between the second liquid alkali pump 31 and the third evaporator 4, the second liquid alkali pump 31 is connected with a tube side inlet of the first tubular heat exchanger 32, and a tube side outlet of the first tubular heat exchanger 32 is connected with a material inlet of the third evaporator 4;
the third caustic soda liquid pump 41 is connected with the shell side inlet of the first tubular heat exchanger 32; the shell side outlet of the first tubular heat exchanger 32 is connected with the heating medium inlet of the second plate heat exchanger 22, and the heating medium outlet of the second plate heat exchanger 22 is connected with the first plate heat exchanger 42;
a steam line 6 is connected in series with the third evaporator 4, the second evaporator 3, the first evaporator 2 and the surface condenser 7 in this order.
In the utility model, the liquid alkali pipeline 1 is input with liquid alkali with low concentration, the concentration is 32%wt, the first evaporator 2 can concentrate 32%wt of liquid alkali into 36%wt of liquid alkali, the second evaporator 3 can concentrate 36%wt of liquid alkali into 42%wt of liquid alkali, and the third evaporator 4 can concentrate 42%wt of liquid alkali into 50%wt of liquid alkali.
In the utility model, the flow direction of the liquid alkali is that 32%wt of liquid alkali (the temperature is room temperature) input by a liquid alkali pipeline 1 sequentially passes through a first evaporator 2, a first liquid alkali pump 21, a second plate heat exchanger 22, a second evaporator 3, a second liquid alkali pump 31, a first tubular heat exchanger 32 and a third evaporator 4 to be concentrated into 50%wt of liquid alkali, the 50%wt of liquid alkali is pressurized by a third liquid alkali pump 41 and then sequentially used for the first tubular heat exchanger 32 and the second plate heat exchanger 22 as heating mediums so as to recycle the heat of the 50%wt of liquid alkali, meanwhile, the temperature of the cooled 50%wt of liquid alkali is reduced, and the cooled 50%wt of liquid alkali is cooled to a preset temperature, such as 45 ℃ by circulating cooling water in the first plate heat exchanger 42 and then can be conveyed to a finished product alkali storage tank 5 for temporary storage.
In the utility model, the flow direction of steam is that the saturated steam with the pressure of 0.85MPa is input into the third evaporator 4 by the steam pipeline 6 to heat and concentrate 42 percent by weight of liquid alkali, and condensed water after the saturated steam with the pressure of 0.85MPa is condensed in the process is input into other working sections to exchange heat again or be utilized. And the steam generated by the heating concentration of 42% of the liquid alkali is output from the third evaporator 4 and enters the second evaporator 3 to heat 36% wt of the liquid alkali in the second evaporator 3. The steam (from the alkali-containing steam generated after 42% wt alkali evaporation and concentration) is condensed into water and output to other working sections for heat exchange or utilization. Whereas the steam generated by the concentration of 36% wt of the liquid alkali by heating is output from the second evaporator 3 and enters the first evaporator 2, and is concentrated by heating for 32% wt of the liquid alkali. The water condensed by the heated steam (from the alkali-containing steam generated after 36% wt of liquid alkali is evaporated and concentrated) can be collected and recycled, while the steam generated by 32% wt of liquid alkali by heating and concentrating is input into the surface condenser 7 for condensation and then is collected and recycled.
A liquid alkali evaporation concentration system has the following working processes:
when in use, the liquid alkali pipeline 1 inputs low-concentration liquid alkali with the concentration of 32%wt into the first evaporator 2 from the material input end of the first evaporator 2, the liquid alkali with the concentration of 36%wt is obtained after heating, evaporating and concentrating, and the 36%wt liquid alkali is heated and input into the second evaporator 3 for evaporating and concentrating after being pressurized by the first liquid alkali pump 21 through the second plate heat exchanger 22.
The 36% wt of liquid caustic soda is concentrated to 42% wt in the second evaporator 3 and then outputted, and the 42% wt of liquid caustic soda outputted from the second evaporator 3 is heated in the tube pass of the first tube heat exchanger 32 after being pressurized by the second liquid caustic soda pump 31 and then is inputted into the third evaporator 4, and is heated and concentrated to 50% wt by the high-pressure raw steam of 0.85MPa inputted through the steam pipeline 6.
The concentrated 50% wt liquid alkali (temperature 140 ℃) is output from the third evaporator 4, enters the shell side of the first tubular heat exchanger 32 as a heating medium to heat 42% wt liquid alkali in the tube side, and the heated 50% wt liquid alkali is output from the shell side of the first tubular heat exchanger 32, enters the second plate heat exchanger 22 as a heating medium to heat 36% wt liquid alkali. The 50% wt of liquid caustic soda heated by 36% wt of liquid caustic soda is output from the second plate heat exchanger 22 and enters the first plate heat exchanger 42, cooled to 45 ℃ by circulating cooling water in the first plate heat exchanger 42, and then conveyed to the finished caustic soda storage tank 5 for storage.
At the same time, the steam line 6 inputs high temperature and high pressure raw steam with the pressure of 0.85MPa into the third evaporator 4, heats 42% wt of liquid alkali entering the third evaporator 4, concentrates the liquid alkali into 50% wt of liquid alkali, condenses the raw steam into steam condensate water (still having a certain heat energy due to higher temperature) for heating other working sections, and then inputs the condensed steam into a working section with high requirement on water quality, such as an electrolysis working section as salt water.
The alkali-containing steam generated after 42% wt of the liquid alkali is heated enters the second evaporator 3, 36% wt of the liquid alkali entering the second evaporator 3 is heated and concentrated, and condensed water generated after the condensation of the steam (from the alkali-containing steam generated after 42% wt of the liquid alkali is evaporated and concentrated) is discharged for centralized treatment.
The alkali-containing steam generated by heating 36% wt of the liquid alkali enters the first evaporator 2, 32% wt of the liquid alkali in the first evaporator 2 is heated, and condensed water generated by condensing the steam (from the alkali-containing steam generated by evaporating and concentrating 36% wt of the liquid alkali) is discharged for centralized treatment.
And the alkali-containing steam generated by heating and concentrating 32% wt of liquid alkali is fed into the surface condenser 7 for condensation and then discharged for centralized treatment.
In the system, high-temperature high-pressure raw steam supplied by a steam pipeline 6 is used as an initial heat source to evaporate and concentrate liquid alkali in a third evaporator 4; the steam generated after the concentration of the liquid alkali in the third evaporator 4 is used as a heat source in the second evaporator 3 to carry out evaporation concentration on the liquid alkali in the second evaporator 3; the steam generated after the liquid alkali in the second evaporator 3 is concentrated is used as a heat source in the first evaporator 2, the liquid alkali in the first evaporator 2 is evaporated and concentrated, namely, the low-concentration liquid alkali output by the liquid alkali pipeline 1 sequentially passes through the first evaporator 2, the second evaporator 3 and the third evaporator 4 to be subjected to gradual heat exchange and concentration to finally obtain the high-concentration liquid alkali with the concentration meeting the standard (near saturated state), the high-concentration liquid alkali output by the third evaporator 4 sequentially passes through the first tubular heat exchanger 32 and the second plate heat exchanger 22, the heat in the high-concentration liquid alkali is used stepwise, the system of the utility model is used by the cooperation of the equipment, the low-concentration liquid alkali at room temperature is evaporated and concentrated step by step to obtain the high-concentration liquid alkali with the standard, and the steam heat energy after the liquid alkali evaporation at each level can be fully utilized, so that the system of the utility model has the beneficial effects of fully utilizing the steam heat, saving the steam usage amount and saving the energy, and overcoming the defect that the steam energy caused by concentrating the liquid alkali to the high-concentration liquid alkali (near saturated state) in the traditional mode of the system of the liquid alkali is not fully utilized.
As shown in fig. 2, the system of the utility model optionally further comprises a third plate heat exchanger 23 and a second tube heat exchanger 33;
the third plate heat exchanger 23 and the second plate heat exchanger 22 are connected with the first liquid caustic pump 21 and the second evaporator 3 in a parallel manner;
the second tubular heat exchanger 33 and the first tubular heat exchanger 32 are connected in parallel with the second liquid caustic pump 31 and the third evaporator 4.
As shown in fig. 3, optionally, the condensate outlet of the third evaporator 4 is connected to the shell side inlet of the second tubular heat exchanger 33; the shell side outlet of the second tubular heat exchanger 33 is connected to the heating medium inlet of the third plate heat exchanger 23.
In the utility model, the third plate heat exchanger 23 and the second plate heat exchanger 22 are connected with the first liquid alkali pump 21 and the second evaporator 3 in a parallel manner, so that 36 wt% of liquid alkali obtained after heating and concentrating by the first evaporator 2 is divided into two paths to be reheated, and one path enters the third plate heat exchanger 23 to be heated by condensate liquid output by the second tubular heat exchanger 33; the other path is fed into the second plate heat exchanger 22 and heated by 50% wt of the liquid caustic outputted from the first tube heat exchanger 32.
Similarly, the second tubular heat exchanger 33 and the first tubular heat exchanger 32 are connected with the second liquid alkali pump 31 and the third evaporator 4 in parallel, so that 42%wt liquid alkali obtained after heating and concentrating by the second evaporator 3 can be divided into two paths to be heated again, one path is the tube side entering the second tubular heat exchanger 33 and is heated by condensate of high-pressure steam condensed in the third evaporator 4, and the condensate after 42%wt liquid alkali heating is then entered into the third plate heat exchanger 23 and 36%wt liquid alkali therein is heated; the other path is the tube side entering the first tube heat exchanger 32 and heated by 50% wt of liquid alkali output by the third evaporator 4.
The connection and distribution mode can fully utilize the heat in 50% wt of liquid alkali and steam condensate, reduce energy waste and heat the liquid alkali to be heated to a proper temperature.
As shown in fig. 3, the system of the present utility model optionally further comprises a condensate storage tank 8, the first evaporator 2, the second evaporator 3, the third evaporator 4 and the surface condenser 7 being connected to the condensate storage tank 8.
In the present utility model, the condensate storage tank 8 is provided to collect and recycle the condensate of the vapor in the first evaporator 2, the second evaporator 3, the third evaporator 4 and the surface condenser 7, for example, as electrolyzed brine.
As shown in fig. 4, optionally, a first choke drain tank 24 is provided between the second evaporator 3 and the condensate storage tank 8;
a second choke drain tank 34 is provided between the third evaporator 4 and the second tubular heat exchanger 33.
The utility model provides a gas-blocking drain tank, which is an important safety device for ensuring the safe operation of an evaporator, and can timely drain condensed water in the tank to prevent the tank body from generating larger stress to cause deformation.
Among them, the condensed water of the third evaporator 4 is available for use as the heating medium of the second tube heat exchanger 33 because the temperature of the steam outputted therefrom is high.
Alternatively, the first plate heat exchanger 42 is one of a flat plate heat exchanger, a hot plate heat exchanger, or a spiral plate heat exchanger.
In the utility model, enterprises can select the plate heat exchangers of different types according to the production conditions and the demands of the enterprises.
Alternatively, the first evaporator 2, the second evaporator 3 and the third evaporator 4 are falling film evaporators.
In the utility model, the falling film evaporator is selected, and the utility model has the advantages of short residence time, large evaporation heat supply coefficient, small pressure drop and less liquid stagnation in the equipment.
A liquid alkali evaporation concentration system has the following working processes:
when in use, the liquid alkali pipeline 1 inputs low-concentration liquid alkali with the concentration of 32%wt into the first evaporator 2 from the material input end of the first evaporator 2, the liquid alkali with the concentration of 36%wt is obtained after heating, evaporating and concentrating, the 36%wt liquid alkali is divided into two paths after being pressurized by the first liquid alkali pump 21, one path is heated by the second plate heat exchanger 22, the other path is heated by the third plate heat exchanger 23, and the 36%wt liquid alkali which passes through the second plate heat exchanger 22 and the third plate heat exchanger 23 is simultaneously input into the second evaporator 3 for evaporating and concentrating.
The 36% wt of liquid alkali is concentrated to 42% wt in the second evaporator 3, then the liquid alkali is output, the 42% wt of liquid alkali output from the second evaporator 3 is pressurized by the second liquid alkali pump 31 and is divided into two paths, one path of liquid alkali enters the tube pass of the first tube heat exchanger 32 to be heated, the other path of liquid alkali enters the tube pass of the second tube heat exchanger 33 to be heated, the 42% wt of liquid alkali heated by the first tube heat exchanger 32 and the second tube heat exchanger 33 is input into the third evaporator 4, and the high-pressure steam with the pressure of 0.85MPa input by the steam pipeline 6 is heated and concentrated to 50% wt.
The concentrated 50% wt liquid alkali (temperature 140 ℃) is output from the third evaporator 4, enters the shell side of the first tubular heat exchanger 32 as a heating medium to heat 42% wt liquid alkali in the tube side, and the heated 50% wt liquid alkali is output from the shell side of the first tubular heat exchanger 32, enters the second plate heat exchanger 22 as a heating medium to heat 36% wt liquid alkali. The 50% wt of liquid caustic soda heated by 36% wt of liquid caustic soda is output from the second plate heat exchanger 22 and enters the first plate heat exchanger 42, cooled to 45 ℃ by circulating cooling water in the first plate heat exchanger 42, and then conveyed to the finished caustic soda storage tank 5 for storage.
At the same time, the steam pipeline 6 inputs high-temperature high-pressure raw steam with the pressure of 0.85MPa into the third evaporator 4, heats 42% wt of liquid caustic entering the third evaporator 4, concentrates the liquid caustic into 50% wt of liquid caustic, condenses the raw steam into raw steam condensate (still having certain heat energy due to higher temperature), inputs the raw steam condensate into the shell side of the second tubular heat exchanger 33 through the second gas-blocking drain tank 34, heats 42% wt of liquid caustic in the tube side of the raw steam condensate, heats the raw steam condensate output from the shell side of the second tubular heat exchanger 33 by utilizing the heat of the raw steam condensate, then inputs the raw steam condensate into the second plate heat exchanger 23, heats 36% wt of liquid caustic therein, realizes the step utilization of the heat contained in the high-temperature high-pressure raw steam condensate, and collects the raw steam condensate after heating 36% wt of liquid caustic, and can be used for a section with high water quality requirement, such as a clean section for electrolysis brine because of high purity.
The alkali-containing steam generated after 42% wt of liquid alkali is heated enters the second evaporator 3, 36% wt of liquid alkali entering the second evaporator 3 is heated and concentrated, and condensed water generated after the condensation of steam (the alkali-containing steam generated after 42% wt of liquid alkali is evaporated and concentrated) is discharged into the condensate storage tank 8 through the first gas-blocking water discharge tank 24 for centralized treatment.
The alkali-containing steam generated by heating 36% wt of liquid alkali enters the first evaporator 2, 32% wt of liquid alkali in the first evaporator 2 is heated, and condensed water generated by condensing steam (from the alkali-containing steam generated by evaporating and concentrating 36% wt of liquid alkali) is input into the condensate storage tank 8 for centralized treatment.
And the alkali-containing steam generated by heating and concentrating 32% wt of liquid alkali is input into the surface condenser 7 for condensation and then is input into the condensate storage tank 8 for concentrated treatment.
Finally, it should be noted that the above embodiments are merely illustrative of the technical solution of the present utility model, and not limiting thereof; although the utility model has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art will appreciate that; the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (7)
1. A liquid alkali evaporation and concentration system, which is characterized by comprising a liquid alkali pipeline (1) and a steam pipeline (6);
the liquid caustic soda pipeline (1) is sequentially connected with a first evaporator (2), a first liquid caustic soda pump (21), a second evaporator (3), a second liquid caustic soda pump (31), a third evaporator (4), a third liquid caustic soda pump (41), a first plate heat exchanger (42) and a finished caustic soda storage tank (5) in series;
a second plate heat exchanger (22) is arranged between the first liquid alkali pump (21) and the second evaporator (3);
a first tubular heat exchanger (32) is arranged between the second liquid alkali pump (31) and the third evaporator (4), the second liquid alkali pump (31) is connected with a tube side inlet of the first tubular heat exchanger (32), and a tube side outlet of the first tubular heat exchanger (32) is connected with a material inlet of the third evaporator (4);
the third liquid caustic pump (41) is connected with a shell side inlet of the first tubular heat exchanger (32); the shell side outlet of the first tubular heat exchanger (32) is connected with the heating medium inlet of the second plate heat exchanger (22), and the heating medium outlet of the second plate heat exchanger (22) is connected with the first plate heat exchanger (42);
the steam pipeline (6) is connected with the third evaporator (4), the second evaporator (3), the first evaporator (2) and the surface condenser (7) in series in sequence.
2. The liquid caustic evaporation and concentration system according to claim 1, characterized in that the system further comprises a third plate heat exchanger (23) and a second tube heat exchanger (33);
the third plate heat exchanger (23) and the second plate heat exchanger (22) are connected with the first liquid alkali pump (21) and the second evaporator (3) in a parallel connection mode;
the second tubular heat exchanger (33) and the first tubular heat exchanger (32) are connected with the second liquid alkali pump (31) and the third evaporator (4) in a parallel mode.
3. The liquid caustic evaporative concentration system according to claim 2, further comprising a condensate storage tank (8), wherein the first evaporator (2), the second evaporator (3), the third evaporator (4) and the surface condenser (7) are all connected to the condensate storage tank (8).
4. -the liquid caustic evaporation concentration system according to claim 3, characterized in that the condensate outlet of the third evaporator (4) is connected with the shell side inlet of the second tubular heat exchanger (33); the shell side outlet of the second tubular heat exchanger (33) is connected with the heating medium inlet of the third plate heat exchanger (23).
5. The liquid caustic evaporation and concentration system according to claim 4, characterized in that a first gas-blocking drainage tank (24) is arranged between the second evaporator (3) and the condensate storage tank (8);
a second gas-blocking water drain tank (34) is arranged between the third evaporator (4) and the second tubular heat exchanger (33).
6. The liquid caustic evaporation concentration system of claim 1, wherein the first plate heat exchanger (42) is one of a flat plate heat exchanger, a hot plate heat exchanger, or a spiral plate heat exchanger.
7. The liquid caustic evaporation concentration system of claim 1 wherein the first evaporator (2), the second evaporator (3) and the third evaporator (4) are all falling film evaporators.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321542459.5U CN220002966U (en) | 2023-06-16 | 2023-06-16 | Liquid alkali evaporation concentration system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321542459.5U CN220002966U (en) | 2023-06-16 | 2023-06-16 | Liquid alkali evaporation concentration system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220002966U true CN220002966U (en) | 2023-11-14 |
Family
ID=88678514
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321542459.5U Active CN220002966U (en) | 2023-06-16 | 2023-06-16 | Liquid alkali evaporation concentration system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220002966U (en) |
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2023
- 2023-06-16 CN CN202321542459.5U patent/CN220002966U/en active Active
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