CN214032102U - Membrane concentration absorption liquid evaporation crystallization system - Google Patents
Membrane concentration absorption liquid evaporation crystallization system Download PDFInfo
- Publication number
- CN214032102U CN214032102U CN202022830412.1U CN202022830412U CN214032102U CN 214032102 U CN214032102 U CN 214032102U CN 202022830412 U CN202022830412 U CN 202022830412U CN 214032102 U CN214032102 U CN 214032102U
- Authority
- CN
- China
- Prior art keywords
- absorption
- liquid
- unit
- absorption unit
- evaporative
- 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.)
- Active
Links
Images
Abstract
The utility model discloses a membrane concentration absorption liquid evaporative crystallization system, which 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 device for preparing steam by heating 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 a separator, the membrane concentration unit, the clear water cache tank and the absorption liquid cache tank. The utility model discloses a film concentration and multistage evaporation absorption unit's evaporation absorption can practice thrift power consumption and steam quantity greatly to the cost is reduced has solved the high problem of current evaporation crystal system energy consumption.
Description
Technical Field
The utility model relates to a waste water recovery handles technical field, especially relates to a membrane concentration absorption liquid evaporation crystallization system.
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 utility model provides a membrane concentration absorption liquid evaporation crystal system is in order to solve above-mentioned technical problem.
In order to achieve the above purpose, the utility model discloses the technical scheme who adopts is:
a membrane concentration absorption liquid evaporation 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 a circulation outlet of the separator is connected with a circulation inlet of the forced circulation heater through a forced circulation pump, a circulation inlet of the separator is connected with a circulation outlet of the forced circulation heater, and a circulation outlet and a 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 pre-absorption 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.
Compared with the prior art, the utility model discloses a power consumption and steam quantity can be practiced thrift greatly in the evaporation absorption of membrane concentration and multistage evaporation absorption unit to the cost is reduced has solved the high problem of current evaporation crystal system energy consumption.
Drawings
Fig. 1 is a schematic structural 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. However, these embodiments are not intended to limit the present invention, and structural, methodical, or functional changes that may be made by one of ordinary skill in the art based on these embodiments are all 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 pre-absorption 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 utility model discloses still include electrically controlled device, electrically controlled device and separator 1, centrifuge 4, forced circulation heater 2, vapour and liquid separator 20 and the intensification are prepared steam device electricity and are connected.
When in use, the utility model discloses can go on according to following step:
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, and continuously absorbs the heat released by the condensation of the secondary steam from the separator 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 gradually evaporated and has higher concentration, 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 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 present invention is limited only by the appended claims.
Claims (8)
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 liquid heat exchanger of the last evaporative absorption unit, the liquid outlet end of the absorber of the same absorber of the last evaporative absorption unit, and the last evaporative absorption unit, 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 pre-absorption 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022830412.1U CN214032102U (en) | 2020-11-30 | 2020-11-30 | Membrane concentration absorption liquid evaporation crystallization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022830412.1U CN214032102U (en) | 2020-11-30 | 2020-11-30 | Membrane concentration absorption liquid evaporation crystallization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214032102U true CN214032102U (en) | 2021-08-24 |
Family
ID=77364090
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022830412.1U Active CN214032102U (en) | 2020-11-30 | 2020-11-30 | Membrane concentration absorption liquid evaporation crystallization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214032102U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112358113A (en) * | 2020-11-30 | 2021-02-12 | 浙江威明环境科技有限公司 | Membrane concentration absorption liquid evaporation crystallization system and method |
-
2020
- 2020-11-30 CN CN202022830412.1U patent/CN214032102U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112358113A (en) * | 2020-11-30 | 2021-02-12 | 浙江威明环境科技有限公司 | Membrane concentration absorption liquid evaporation crystallization system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103466736B (en) | A kind of circulating treating system of high-concentration salt-containing wastewater and technique | |
| CN105923676A (en) | Efficient solar seawater desalination and air conditioner refrigeration combined operation method and system thereof | |
| CN112358113A (en) | Membrane concentration absorption liquid evaporation crystallization system and method | |
| CN117185389A (en) | Concentrated crystallization desalination water treatment facilities of high salt waste water will contain through lithium bromide unit | |
| CN111115735A (en) | Two-stage forced circulation evaporation system and process for landfill leachate | |
| CN214032102U (en) | Membrane concentration absorption liquid evaporation crystallization system | |
| CN113932474A (en) | Heat pump multiple-effect evaporation coupling type water treatment system and working method thereof | |
| CN209922933U (en) | Sodium chloride forced circulation crystallization device in flue gas desulfurization waste water | |
| CN111620402A (en) | System and method for high-salinity wastewater through photo-thermal evaporation crystallization | |
| EP2549205A2 (en) | Triple-effect vapor absorption refrigeration system | |
| CN217287198U (en) | MVR evaporation concentration system | |
| CN212594042U (en) | Two-section type negative pressure evaporation concentration purification treatment device for food-grade waste phosphoric acid | |
| CN202072574U (en) | Ammonium nitrate waste water processing unit | |
| CN111517400B (en) | Low-grade heat source coupling multi-effect flash evaporation concentration evaporation system | |
| CN212476173U (en) | Treatment system for zero discharge of desulfurization wastewater of coal-fired power plant | |
| CN211871447U (en) | Two-stage forced circulation evaporation system for landfill leachate | |
| CN210419272U (en) | Electroplate high salt waste water crystallization salt separation purification energy comprehensive utilization system | |
| CN111514599A (en) | Two-section type negative pressure evaporation concentration purification treatment process and device for food-grade waste phosphoric acid | |
| CN108609786B (en) | Evaporation condensation circulation equipment and method for driving brine separation and full recovery of high-salt wastewater by low-quality waste heat | |
| CN111362339A (en) | A concentrated atomizing evaporation to dryness equipment for desulfurization waste water | |
| CN218011111U (en) | Efficient steam distribution and two-stage compressor series MVR evaporation separation device | |
| CN214570869U (en) | Industrial wastewater separation and waste heat recovery system applying solar energy and lithium bromide heat pump | |
| CN218058514U (en) | Precursor mother liquor processing system | |
| CN112919567B (en) | Riboflavin fermentation waste water evaporation crystallization system | |
| CN219318683U (en) | Waste heat recycling system of mixed salt mother liquor drying device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |