CN112358113A - Membrane concentration absorption liquid evaporation crystallization system and method - Google Patents
Membrane concentration absorption liquid evaporation crystallization system and method Download PDFInfo
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- CN112358113A CN112358113A CN202011376725.2A CN202011376725A CN112358113A CN 112358113 A CN112358113 A CN 112358113A CN 202011376725 A CN202011376725 A CN 202011376725A CN 112358113 A CN112358113 A CN 112358113A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/10—Bromides
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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Abstract
The invention discloses a membrane concentration absorption liquid evaporative crystallization system and a membrane concentration absorption liquid evaporative crystallization method, wherein the membrane concentration absorption liquid evaporative crystallization system comprises a separator with a wastewater inlet and a steam outlet, a centrifugal machine, a forced circulation heater, a gas-liquid separator and a temperature rise steam preparation device, wherein the separator is connected with the forced circulation heater through a forced circulation pump, the separator is connected with the forced circulation heater, and the separator is connected with the centrifugal machine; the temperature-rising steam preparation device comprises a clear water cache tank, an absorption liquid cache tank, a membrane concentration unit and an evaporation absorption unit, wherein the membrane concentration unit is respectively connected with the clear water cache tank and the absorption liquid cache tank, and the evaporation absorption unit is respectively connected with the separator, the membrane concentration unit, the clear water cache tank and the absorption liquid cache tank; corresponding methods are also disclosed. According to the invention, through membrane concentration and evaporation absorption of the multi-stage evaporation absorption unit, the power consumption and the steam consumption can be greatly saved, so that the cost is reduced, and the problem of high energy consumption of the existing evaporation crystallization system is solved.
Description
Technical Field
The invention relates to the technical field of wastewater recovery treatment, in particular to a membrane concentration absorption liquid evaporation crystallization system and a membrane concentration absorption liquid evaporation crystallization method.
Background
The evaporative crystallization device is widely applied to the treatment of wastewater in the industries of chemical industry, nonferrous metals, pesticides, food, pharmacy, desulfurization, mine smelting, steel plants, oil fields and the like, the pure environmental protection treatment and the standard discharge are deepened into the environmental protection treatment and the comprehensive utilization through the recovery of soluble salt in the wastewater, and ammonium chloride, potassium chloride, ammonium sulfate and the like in the wastewater are crystallized and recycled.
However, the evaporative crystallization device is a high-energy-consumption device, a large amount of heat energy or electric energy is consumed for evaporating one ton of water, and the reduction of steam and electric energy consumption of a high-salt wastewater crystallization system is an urgent problem. The most widely adopted technologies at present are a multi-effect evaporation crystallization system and an MVR evaporation crystallization system (secondary vapor recompression), for example, the water generation ratio of the double-effect evaporation system is 1.5, that is, one ton of steam is consumed when 1.5 tons of wastewater is evaporated, and for example, about 75KW of electric energy is consumed when 1 ton of water is evaporated by the MVR evaporation crystallization system. China is a big coal-fired thermal power country, consumes a large amount of heat energy or electric energy in the process of wastewater treatment, increases the coal-fired quantity in a phase-changing manner, causes pollution to the environment, and the treatment of high-salinity wastewater is an important environmental protection problem.
Disclosure of Invention
The invention provides a membrane concentration absorption liquid evaporation crystallization system and a membrane concentration absorption liquid evaporation crystallization method to solve the technical problems.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
according to the first aspect of the embodiment of the invention, the membrane concentrated absorption liquid evaporative crystallization system comprises a separator with a wastewater inlet and a steam outlet, a centrifugal machine, a forced circulation heater with a steam inlet and a condensed water outlet, a gas-liquid separator and a temperature rise steam preparation device, wherein the circulation outlet of the separator is connected with the circulation inlet of the forced circulation heater through a forced circulation pump, the circulation inlet of the separator is connected with the circulation outlet of the forced circulation heater, and the circulation outlet and the recovery inlet of the separator are both connected with the centrifugal machine;
the temperature-rising steam preparation device comprises a clear water cache tank, an absorption liquid cache tank, a membrane concentration unit and an evaporation absorption unit, wherein the membrane concentration unit is respectively connected with the clear water cache tank and the absorption liquid cache tank through pipelines, and the evaporation absorption unit is respectively connected with the separator, the membrane concentration unit, the clear water cache tank and the absorption liquid cache tank through pipelines; the evaporation absorption unit is used for absorbing the water vapor evaporated from the separator through absorption liquid and releasing heat, and the membrane concentration unit is used for concentrating and regenerating the absorption liquid of the evaporation absorption unit.
Preferably, the evaporation absorption unit comprises a primary evaporation absorption unit, at least one intermediate evaporation absorption unit and a final evaporation absorption unit which are sequentially arranged, the primary evaporation absorption unit, the intermediate evaporation absorption unit and the final evaporation absorption unit respectively comprise an evaporator and an absorber, and the water supply end of each evaporator is connected with the fresh water buffer tank; a steam inlet of the primary evaporation absorption unit evaporator is connected with a steam outlet of the separator through a pipeline, a condensed water outlet of the primary evaporation absorption unit evaporator is connected with a gas-liquid separator, and a heat supply end of the primary evaporation absorption unit evaporator is connected with an industrial waste heat source; the heat supply ends of the evaporators of the intermediate-stage evaporation absorption unit and the final-stage evaporation absorption unit are respectively connected to the heat output end of the absorber of the previous-stage evaporation absorption unit; liquid supply ends of absorbers of the primary evaporation absorption unit and the middle evaporation absorption unit are respectively connected to a liquid outlet end of an absorber of the next evaporation absorption unit, and a liquid supply end of an absorber of the last evaporation absorption unit is connected with the membrane concentration unit.
Preferably, the evaporation absorption unit further comprises an absorption liquid heat exchanger, the absorption liquid heat exchanger of the primary evaporation absorption unit is respectively connected with the absorption liquid buffer tank, the membrane concentration unit, the liquid outlet end of the primary evaporation absorption unit absorber and the absorption liquid heat exchanger of the next-stage evaporation absorption unit, the absorption liquid heat exchanger of each intermediate-stage evaporation absorption unit is respectively connected with the liquid supply end of the first-stage evaporation absorption unit absorber, the absorption liquid heat exchanger of the previous-stage evaporation absorption unit, the liquid outlet end of the same-stage evaporation absorption unit absorber and the absorption liquid heat exchanger of the next-stage evaporation absorption unit, the absorption liquid heat exchanger of the last stage evaporation absorption unit is respectively connected with the liquid supply end of the absorber of the first stage evaporation absorption unit, the absorption liquid heat exchanger of the previous stage evaporation absorption unit, the liquid outlet end of the absorber of the same stage evaporation absorption unit and the liquid supply end of the absorber of the same stage evaporation absorption unit.
Preferably, the membrane concentration unit comprises a membrane module, a module security cooler and a pre-absorption cooler, the membrane module is connected with the post-absorption pre-cooler and then respectively connected with the clear water cache tank and the absorption liquid cache tank through pipelines, the module security cooler is provided with a circulating cooling water inlet and outlet, and the module security cooler is connected with the pre-absorption cooler.
Preferably, a regulating valve is arranged on a pipeline connecting the membrane module and the evaporation absorption unit.
Preferably, the temperature of the industrial waste heat source is greater than or equal to 90 ℃.
Preferably, the system also comprises an electric control device which is electrically connected with the separator, the centrifuge, the forced circulation heater, the gas-liquid separator and the temperature rise steam preparation device.
Preferably, the absorbing solution is an aqueous solution of lithium bromide, lithium chloride or a compound of lithium bromide and ammonia.
According to a second aspect of the embodiments of the present invention, there is provided a method for evaporative crystallization of lithium bromide concentrated by a membrane, comprising the following steps:
step 101: the high-salinity wastewater is continuously heated in a circulating way among the separator, the forced circulation heater and the forced circulation pump, and the water is continuously evaporated;
step 102: the water vapor evaporated from the separator passes through a plurality of evaporation absorption units consisting of an evaporator and an absorber in turn, the water vapor from the evaporator in each evaporation absorption unit is absorbed by absorption liquid in the absorber and releases heat, and the absorption liquid is sprayed from the absorber of the next unit or concentrated from a membrane module;
step 103: the water vapor in the last absorber is absorbed and the released heat is used for heating the water condensed out by the forced circulation heater, so that the water is changed into low-pressure steam again and is sent to the forced circulation heater for heating the high-salinity wastewater;
step 104: concentrating and regenerating the absorption liquid of the first absorber through a membrane concentration unit;
step 105: the high-salt wastewater in the separator finally becomes saturated solution and salt crystals are separated out due to continuous evaporation of water, the wastewater containing the salt crystals is conveyed to a centrifugal machine for separation, the separated salt is recycled, and the liquid separated from the centrifugal machine is conveyed to the separator again for evaporation and crystallization.
Compared with the prior art, the invention can greatly save the power consumption and the steam consumption through the membrane concentration and the evaporation absorption of the multi-stage evaporation absorption unit, thereby reducing the cost and solving the problem of high energy consumption of the existing evaporation crystallization system.
Drawings
FIG. 1 is a schematic diagram of a membrane-concentrated absorption liquid evaporative crystallization system according to the present invention.
In the figure, 1-separator, 2-forced circulation heater, 3-forced circulation pump, 4-centrifuge, 5-primary evaporator, 6-secondary evaporator, 7-final evaporator, 8-primary absorber, 9-secondary absorber, 10-final absorber, 11-primary absorption liquid heat exchanger, 12-secondary absorption liquid heat exchanger, 13-final absorption liquid heat exchanger, 14-clear water buffer tank, 15-absorption liquid buffer tank, 16-membrane module, 17-pre-absorption cooler, 18-module security cooler, 19-regulating valve and 20-gas-liquid separator.
Detailed Description
The present invention will be described in detail below with reference to specific embodiments shown in the drawings. These embodiments are not intended to limit the present invention, and structural, methodological, or functional changes made by those skilled in the art according to these embodiments are included in the scope of the present invention.
The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used in this specification and the appended claims, the singular forms "a", "an", and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It should also be understood that the term "and/or" as used herein refers to and encompasses any and all possible combinations of one or more of the associated listed items.
As shown in fig. 1, a membrane concentrated absorption liquid evaporative crystallization system comprises a separator 1 with a wastewater inlet and a steam outlet, a centrifuge 4, a forced circulation heater 2 with a steam inlet and a condensed water outlet, a gas-liquid separator 20 and a temperature rise steam preparation device, wherein the circulation outlet of the separator 1 is connected with the circulation inlet of the forced circulation heater through a forced circulation pump 3, the circulation inlet of the separator 1 is connected with the circulation outlet of the forced circulation heater 2, and the circulation outlet and the recovery inlet of the separator 1 are both connected with the centrifuge 4; the temperature-rising steam preparation device comprises a clear water cache tank 14, an absorption liquid cache tank 15, a membrane concentration unit and an evaporation absorption unit, wherein the membrane concentration unit is respectively connected with the clear water cache tank 14 and the absorption liquid cache tank 15 through pipelines, and the evaporation absorption unit is respectively connected with a separator, the membrane concentration unit, the clear water cache tank and the absorption liquid cache tank through pipelines; the evaporation absorption unit is used for absorbing the water vapor evaporated from the separator through the absorption liquid and releasing heat, and the membrane concentration unit is used for concentrating and regenerating the absorption liquid of the evaporation absorption unit.
The evaporation absorption unit can comprise a primary evaporation absorption unit, at least one intermediate evaporation absorption unit and a final evaporation absorption unit which are sequentially arranged, the primary evaporation absorption unit, the intermediate evaporation absorption unit and the final evaporation absorption unit respectively comprise an evaporator and an absorber, and the water supply end of each evaporator is connected with the fresh water cache tank 14; a steam inlet of a primary evaporator 5 of the primary evaporation absorption unit is connected with a steam outlet of the separator through a pipeline, a condensed water outlet of the primary evaporator 5 is connected with a gas-liquid separator, and a heat supply end of the primary evaporator 5 is connected with an industrial waste heat source; the heat supply ends of the evaporators of the intermediate-stage evaporation absorption unit and the final-stage evaporation absorption unit are respectively connected to the heat output end of the absorber of the previous-stage evaporation absorption unit; liquid supply ends of absorbers of the primary evaporation absorption unit and the middle evaporation absorption unit are respectively connected to a liquid outlet end of an absorber of the next evaporation absorption unit, and a liquid supply end of an absorber of the last evaporation absorption unit is connected with the membrane concentration unit. The industrial waste heat source refers to heat energy which is discharged in the production and manufacture of the industries such as chemical industry, nonferrous metals, pesticides, foods, pharmacy, desulfurization, mine smelting, steel mills, oil fields and the like and is not recycled, and can also be replaced by other heat sources which can be effectively utilized.
In order to maintain the heat balance, the evaporation absorption unit can also comprise an absorption liquid heat exchanger, the absorption liquid heat exchanger of the primary evaporation absorption unit is respectively connected with an absorption liquid buffer tank 15, a membrane concentration unit, the liquid outlet end of the primary evaporation absorption unit absorber and the absorption liquid heat exchanger of the next evaporation absorption unit, the absorption liquid heat exchanger of each intermediate evaporation absorption unit is respectively connected with the liquid supply end of the first evaporation absorption unit absorber, the absorption liquid heat exchanger of the previous evaporation absorption unit, the liquid outlet end of the same evaporation absorption unit absorber and the absorption liquid heat exchanger of the next evaporation absorption unit, the absorption liquid heat exchanger of the last stage evaporation absorption unit is respectively connected with the liquid supply end of the absorber of the first stage evaporation absorption unit, the absorption liquid heat exchanger of the previous stage evaporation absorption unit, the liquid outlet end of the absorber of the same stage evaporation absorption unit and the liquid supply end of the absorber of the same stage evaporation absorption unit. Through the absorption liquid heat exchanger, the dilute solution of the absorption liquid flowing out of each stage of absorption liquid and the concentrated solution of the absorption liquid concentrated and regenerated by the membrane concentration unit can exchange heat, so that the dilute solution of the absorption liquid is preheated before concentration, and the concentrated solution of the absorption liquid is cooled firstly before returning.
Here, the absorption liquid may be an aqueous solution of lithium bromide, lithium chloride or a compound of lithium bromide and ammonia, and the temperature of the industrial waste heat source is required to be 90 ℃ or higher. The number of the intermediate-stage evaporation and absorption units can be set according to actual needs, and only one intermediate-stage evaporation and absorption unit (i.e. two-stage evaporation and absorption unit) is exemplified here.
The membrane concentration unit can comprise a membrane module 16, a module security cooler 18 and a pre-absorption cooler 17, wherein the membrane module 16 is connected with the post-absorption pre-cooler 17 and then respectively connected with the clear water cache tank 14 and the absorption liquid cache tank 15 through pipelines, the module security cooler 18 is provided with a circulating cooling water inlet and outlet, and the module security cooler 18 is connected with the pre-absorption cooler 17. In order to ensure the installation and operation of the membrane module, the membrane module 16 has certain requirements on the operation temperature, and the temperature cannot be too high, the cooler 17 before absorption can exchange heat between the high-temperature dilute solution to be treated and the low-temperature clear water produced by the membrane module 16, so that the maximum heat efficiency of the system is ensured; the modular safety cooler 18 ensures that the dilute solution entering the membrane module is not damaged by the excessive temperature of the absorption liquid.
In order to control the amount and concentration of the concentrated absorption solution concentrated and regenerated by the membrane concentration unit and returned to the evaporation absorption unit, a regulating valve 19 can be arranged on a pipeline connecting the membrane module 16 and the evaporation absorption unit, wherein the regulating valve 19 can be an electric control valve.
In order to facilitate the automatic control of the whole process flow, the invention also comprises an electric control device which is electrically connected with the separator 1, the centrifuge 4, the forced circulation heater 2, the gas-liquid separator 20 and the temperature-rising steam preparation device.
Based on the membrane concentration absorption liquid evaporative crystallization system, the invention also provides a membrane concentration lithium bromide evaporative crystallization method, which comprises the following steps:
step 101: the high-salinity wastewater is continuously heated in a circulating way among the separator 1, the forced circulation heater 2 and the forced circulation pump 3, and the water is continuously evaporated.
The high-salinity wastewater to be treated enters the separator 1 through a pipeline for evaporation and crystallization. Under the circulation action of the separator 1, the forced circulation heater 2 and the forced circulation pump 3, the moisture of the high-salinity wastewater is continuously evaporated and introduced into the evaporation absorption unit.
Step 102: the water vapor evaporated from the separator passes through a plurality of evaporation absorption units consisting of an evaporator and an absorber in turn, the water vapor from the evaporator in each evaporation absorption unit is absorbed by absorption liquid in the absorber and releases heat, and the absorption liquid is sprayed from the absorber of the latter unit or concentrated from a membrane module.
Hereinafter, the intermediate-stage evaporation and absorption unit will be briefly described as having only the two-stage evaporation and absorption unit. If a plurality of intermediate-stage evaporation absorption units exist, the related functional processes of the secondary evaporation absorption units are repeated.
The water vapour evaporated in the separator is piped to the primary evaporator 5 for condensation. In the primary evaporator 5, steam from the separator 1 is condensed into clean distilled water, the distilled water is subjected to gas-liquid separation through a gas-liquid separator 20 and then is discharged out of a system for recycling, and noncondensable gas separated from the water is separately treated; in the primary evaporator 5, the water in the fresh water buffer tank 14 is continuously conveyed to the primary evaporator 5 through the evaporation pump, continuously absorbs the heat released by the condensation of the secondary steam from the separator 1 and continuously evaporates into water vapor.
The water vapor in the primary evaporator 5 is conveyed into the primary absorber 8 through a pipeline, the water vapor in the primary absorber 8 is continuously absorbed by the absorption liquid sprayed down by the secondary absorber 9 and releases heat, the concentration of the absorption liquid after absorbing the water vapor is continuously reduced, the capacity of absorbing the water vapor is continuously reduced, and the absorption liquid dilute solution is conveyed into the absorption liquid buffer tank 15 through a pipeline.
In the primary absorber 8, the water vapor is absorbed by the absorption liquid to release heat, and the heat is transferred to the secondary evaporator 6 through a heat transfer device. In the secondary evaporator 6, the water in the fresh water buffer tank 14 is continuously conveyed to the secondary evaporator 6 by the evaporation pump and continuously absorbs the heat conveyed by the primary absorber 8 and is continuously evaporated into water vapor. In this case, the temperature of the steam generated by the secondary evaporator 6 is much higher than that of the steam generated by the primary evaporator 5.
The water vapor in the secondary evaporator 6 is conveyed to the secondary absorber 9 through a pipeline, the water vapor in the secondary absorber 9 is continuously absorbed by the absorption liquid sprayed down by the final absorber 10 and releases heat, the concentration of the absorption liquid is reduced after the absorption liquid absorbs the water vapor, and the absorption liquid is conveyed to the primary absorber 8 to absorb the water vapor with the relatively lower temperature.
In the secondary absorber 9, the water vapour is absorbed by the absorption liquid and releases heat, which is transferred to the final evaporator 7 by the means for causing the heat to be transferred. In the last evaporator 7, the water in the fresh water buffer tank 14 is continuously conveyed to the last evaporator 7 by the evaporation pump and continuously absorbs the heat conveyed by the second-stage absorber 9 and is continuously evaporated into water vapor. In this case, the steam temperature generated by the final stage evaporator 7 is much higher than that generated by the second stage evaporator 6.
The water vapor in the final stage evaporator 7 is conveyed to the final stage absorber 10 through a pipeline, the water vapor in the final stage absorber 10 is continuously concentrated by the membrane component 16 and then conveyed to the absorption liquid concentrated solution, the concentration of the absorption liquid concentrated solution is reduced after the absorption liquid absorbs the water vapor, and the absorption liquid is conveyed to the secondary absorption 9 to absorb the water vapor of a relatively lower temperature stage.
Step 103: and the water vapor in the last absorber is absorbed to release heat to heat the water condensed out by the forced circulation heater, so that the water is changed into low-pressure steam again and is sent to the forced circulation heater to heat the high-salinity wastewater.
In the final absorber 10, the water vapor is absorbed by the strong solution of the absorption liquid to release heat continuously, and the heat is used for heating the water condensed out by the forced circulation heater 2, so that the water is changed into low-pressure steam again and is conveyed into the forced circulation heater 2 again to heat the high-salinity wastewater.
Step 104: and concentrating and regenerating the absorption liquid of the first absorber through a membrane concentration unit.
In the primary absorber 8, the absorption liquid has become very dilute, and the absorption capacity for water vapor becomes very small, so that the absorption liquid is subjected to the concentration regeneration treatment by the membrane module 16. The absorption liquid dilute solution is sent to the membrane module 16 in the absorption liquid buffer tank 15 by the absorption liquid feed pump to be concentrated and separated. The concentration of the absorbent solution can be adjusted and controlled by adjusting valve 19 that can adjust the absorbent concentrate. The concentrated absorption solution from the membrane module 16 is sent to the final absorber 10 again to absorb water vapor. Clean water generated by the membrane module 16 is conveyed to the clean water buffer tank 14 to be conveyed to each stage of evaporator again for evaporation and heat transfer.
Step 105: the high-salt waste water in the separator 1 is at higher concentration due to continuous evaporation of water, and finally becomes saturated solution and salt crystals are separated out, the waste water containing the salt crystals is conveyed to the centrifuge 4 to be separated, the separated salt (industrial salt) is recycled, and the liquid separated from the centrifuge 4 is conveyed to the separator 1 again to be evaporated and crystallized.
Other embodiments of the invention will be apparent to those skilled in the art from consideration of the specification and practice of the invention disclosed herein. This application is intended to cover any variations, uses, or adaptations of the invention following, in general, the principles of the invention and including such departures from the present disclosure as come within known or customary practice within the art to which the invention pertains. It is intended that the specification and examples be considered as exemplary only, with a true scope and spirit of the invention being indicated by the following claims.
It will be understood that the invention is not limited to the precise arrangements described above and shown in the drawings and that various modifications and changes may be made without departing from the scope thereof. The scope of the invention is limited only by the appended claims.
Claims (9)
1. A membrane concentration absorption liquid evaporation crystallization system is characterized by comprising a separator with a wastewater inlet and a steam outlet, a centrifugal machine, a forced circulation heater with a steam inlet and a condensed water outlet, a gas-liquid separator and a temperature rise steam preparation device, wherein the circulation outlet of the separator is connected with the circulation inlet of the forced circulation heater through a forced circulation pump, the circulation inlet of the separator is connected with the circulation outlet of the forced circulation heater, and the circulation outlet and the recovery inlet of the separator are both connected with the centrifugal machine;
the temperature-rising steam preparation device comprises a clear water cache tank, an absorption liquid cache tank, a membrane concentration unit and an evaporation absorption unit, wherein the membrane concentration unit is respectively connected with the clear water cache tank and the absorption liquid cache tank through pipelines, and the evaporation absorption unit is respectively connected with the separator, the membrane concentration unit, the clear water cache tank and the absorption liquid cache tank through pipelines; the evaporation absorption unit is used for absorbing the water vapor evaporated from the separator through absorption liquid and releasing heat, and the membrane concentration unit is used for concentrating and regenerating the absorption liquid of the evaporation absorption unit.
2. The evaporative crystallization system for membrane concentrated absorption liquid according to claim 1, wherein the evaporative absorption unit comprises a primary evaporative absorption unit, at least one intermediate evaporative absorption unit and a final evaporative absorption unit which are arranged in sequence, the primary evaporative absorption unit, the intermediate evaporative absorption unit and the final evaporative absorption unit respectively comprise an evaporator and an absorber, and the water supply end of each evaporator is connected with the fresh water buffer tank; a steam inlet of the primary evaporation absorption unit evaporator is connected with a steam outlet of the separator through a pipeline, a condensed water outlet of the primary evaporation absorption unit evaporator is connected with a gas-liquid separator, and a heat supply end of the primary evaporation absorption unit evaporator is connected with an industrial waste heat source; the heat supply ends of the evaporators of the intermediate-stage evaporation absorption unit and the final-stage evaporation absorption unit are respectively connected to the heat output end of the absorber of the previous-stage evaporation absorption unit; liquid supply ends of absorbers of the primary evaporation absorption unit and the middle evaporation absorption unit are respectively connected to a liquid outlet end of an absorber of the next evaporation absorption unit, and a liquid supply end of an absorber of the last evaporation absorption unit is connected with the membrane concentration unit.
3. The evaporative crystallization system for membrane-concentrated absorption liquid according to claim 2, wherein the evaporative absorption unit further comprises an absorption liquid heat exchanger, the absorption liquid heat exchanger of the primary evaporative absorption unit is connected to the absorption liquid buffer tank, the membrane concentration unit, the liquid outlet end of the absorber of the primary evaporative absorption unit and the absorption liquid heat exchanger of the next evaporative absorption unit, the absorption liquid heat exchanger of each intermediate evaporative absorption unit is connected to the liquid supply end of the absorber of the first evaporative absorption unit, the absorption liquid heat exchanger of the previous evaporative absorption unit, the liquid outlet end of the absorber of the same evaporative absorption unit and the absorption liquid heat exchanger of the next evaporative absorption unit, the absorption liquid heat exchanger of the last evaporative absorption unit is connected to the liquid supply end of the absorber of the previous evaporative absorption unit, the liquid outlet end of the absorber of the same evaporative absorption unit, the, The liquid supply end of the absorber of the same stage of evaporation absorption unit.
4. The evaporative crystallization system for membrane-concentrated absorption liquid according to claim 1, wherein the membrane concentration unit comprises a membrane module, a modular emergency cooler and a pre-absorption cooler, the membrane module is connected with the post-absorption pre-cooler and then respectively connected with the fresh water buffer tank and the absorption liquid buffer tank through pipes, the modular emergency cooler has a circulating cooling water inlet and outlet, and the modular emergency cooler is connected with the pre-absorption cooler.
5. The evaporative crystallization system for membrane-concentrated absorption liquid according to claim 4, wherein the pipeline connecting the membrane module and the evaporative absorption unit is provided with a regulating valve.
6. The membrane concentrated absorption liquid evaporative crystallization system of claim 2, wherein the temperature of the industrial waste heat source is greater than or equal to 90 ℃.
7. The evaporative crystallization system for membrane concentrated absorption liquid according to any one of claims 1 to 6, further comprising an electric control device electrically connected to the separator, the centrifuge, the forced circulation heater, the gas-liquid separator and the temperature-raising steam-making device.
8. The membrane concentrated absorption liquid evaporative crystallization system according to any one of claims 1 to 6, wherein the absorption liquid is an aqueous solution of lithium bromide, lithium chloride or a compound formed by lithium bromide and ammonia.
9. A membrane concentration lithium bromide evaporation crystallization method is characterized by comprising the following steps:
step 101: the high-salinity wastewater is continuously heated in a circulating way among the separator, the forced circulation heater and the forced circulation pump, and the water is continuously evaporated;
step 102: the water vapor evaporated from the separator passes through a plurality of evaporation absorption units consisting of an evaporator and an absorber in turn, the water vapor from the evaporator in each evaporation absorption unit is absorbed by absorption liquid in the absorber and releases heat, and the absorption liquid is sprayed from the absorber of the next unit or concentrated from a membrane module;
step 103: the water vapor in the last absorber is absorbed and the released heat is used for heating the water condensed out by the forced circulation heater, so that the water is changed into low-pressure steam again and is sent to the forced circulation heater for heating the high-salinity wastewater;
step 104: concentrating and regenerating the absorption liquid of the first absorber through a membrane concentration unit;
step 105: the high-salt wastewater in the separator finally becomes saturated solution and salt crystals are separated out due to continuous evaporation of water, the wastewater containing the salt crystals is conveyed to a centrifugal machine for separation, the separated salt is recycled, and the liquid separated from the centrifugal machine is conveyed to the separator again for evaporation and crystallization.
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| CN113461033A (en) * | 2021-07-21 | 2021-10-01 | 易卫 | Dechlorination process for lithium bromide solution |
| CN114602878A (en) * | 2022-03-31 | 2022-06-10 | 中化(浙江)膜产业发展有限公司 | Online cleaning system of evaporative crystallization device |
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