CN116081741A - Garbage leachate doublestage MVR evaporation crystallizer - Google Patents

Garbage leachate doublestage MVR evaporation crystallizer Download PDF

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CN116081741A
CN116081741A CN202211671610.5A CN202211671610A CN116081741A CN 116081741 A CN116081741 A CN 116081741A CN 202211671610 A CN202211671610 A CN 202211671610A CN 116081741 A CN116081741 A CN 116081741A
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primary
outlet
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inlet
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胡继忠
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Jiangyin Jiangzhong Equipment Manufacturing Co ltd
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Jiangyin Jiangzhong Equipment Manufacturing Co ltd
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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
    • C02F1/08—Thin film evaporation
    • 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
    • C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/10—Energy recovery

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

The invention discloses a garbage leachate two-stage MVR evaporation crystallizer which comprises a first-stage evaporation concentrator, wherein the first-stage evaporation concentrator comprises a first-stage separator, a first-stage heater, a first-stage circulating pump, a first-stage discharging pump, a first-stage gas washing tower and a first-stage compressor; the second-stage circulation evaporation crystallizer comprises a second-stage separator, a second-stage circulation pump, a first second-stage heater, a second-stage heater, a second-stage scrubber, a second-stage compressor and a second-stage discharge pump; a solid-liquid separation assembly; a primary condensate water treatment assembly; and a secondary condensate water treatment assembly. This landfill leachate doublestage MVR evaporation crystallizer is concentrated and evaporative crystallization handles waste liquid evaporation in proper order through one-level evaporation concentrator and second grade circulation evaporation crystallizer, utilizes one-level comdenstion water treatment component to collect the comdenstion water wash gas that the heat medium formed and preheat the waste liquid, utilizes the comdenstion water wash gas that the heat medium formed is collected to the second grade comdenstion water treatment component, reduces the water consumption by a wide margin, reduces running cost, and is more energy-concerving and environment-protective.

Description

Garbage leachate doublestage MVR evaporation crystallizer
Technical Field
The invention relates to the technical field of MVR evaporation crystallization, in particular to a garbage leachate double-stage MVR evaporation crystallizer.
Background
The landfill leachate is high-concentration organic wastewater with complex components, and has the following characteristics: 1. the water quality is complex and the hazard is large; 2. COD and BOD concentration are high; 3. the ammonia nitrogen content is high; 4. the water quality is greatly changed; 5. high metal content, etc. In particular, the COD and TDS content in the high-concentration landfill leachate is high, and biochemical treatment cannot be adopted. If the waste water is directly evaporated and crystallized, high-cost components are gradually enriched in the evaporation and concentration process, the burden of an evaporation system is greatly increased, a large amount of concentrated solution is discharged to cause environmental pollution, and the independent treatment can increase the treatment energy consumption, so that the treatment cost is too high and the economical efficiency is poor.
The Chinese patent publication No. CN218011111U discloses a vapor efficient distribution and two-stage compressor serial MVR evaporation separation device, which comprises a preheating unit, a low-temperature evaporation crystallization low-boiling salt unit, a high-temperature evaporation crystallization high-boiling salt unit, a low-temperature vapor compression unit, a high-temperature vapor compression unit and a condensate water unit. The device effectively distributes heat exchange temperature difference through adopting the technology of two-stage efficient energy-saving mechanical steam recompressors in series, realizes the efficient utilization of steam, and the energy consumption of the evaporation system for producing 1t of water is about 1/6 to 1/5 of that of the traditional evaporator, so that the external steam consumption is less, the dependence on steam equipment such as a boiler is reduced, the use limit of the traditional MVR system is expanded, the emission of pollutants is reduced, the device is more energy-saving and environment-friendly, the device is easy to realize, the automation degree is high, and the operation cost is low.
However, in the operation process of the evaporation separation device, cooling water needs to be continuously introduced, so that the water cost of the device is increased; and the heat of the raw steam is not fully utilized, so that a large amount of raw steam is required to be introduced when evaporation and crystallization are required, and the treatment cost is further increased; in addition, before entering the separator, the waste water stock solution is not subjected to purification treatment, and bubbles are mixed in the stock solution, so that the heat exchange efficiency of the stock solution is reduced, and in the evaporation process, the structure is easily attached to the inner wall of the evaporator, the heat transfer is affected, the energy consumption of the device is further increased, and the treatment efficiency is reduced.
Therefore, there is a need for an improvement in the prior art landfill leachate dual stage MVR evaporative crystallizer.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide the garbage leachate two-stage MVR evaporation crystallizer which reduces water consumption, reduces energy consumption and improves evaporation efficiency.
In order to achieve the technical effects, the technical scheme of the invention is as follows: a landfill leachate doublestage MVR evaporation crystallizer, includes:
the primary evaporation concentrator comprises a primary separator, a primary heater, a primary circulating pump, a primary discharging pump, a primary gas washing tower and a primary compressor, wherein the primary separator is provided with a primary separation inlet, a primary separation outlet and a primary secondary steam outlet, the primary separation outlet is communicated with the primary separation inlet through the primary circulating pump and the primary heater in sequence, the primary gas washing tower is provided with a primary secondary steam inlet and a primary gas outlet, the primary secondary steam outlet is communicated with the primary secondary steam inlet, the primary gas outlet is communicated with a heating medium inlet of the primary heater through the primary compressor, and the heating medium inlet of the primary heater is also used for being connected with a generating steam source;
The secondary circulation evaporation crystallizer comprises a secondary separator, a secondary circulation pump, a first secondary heater, a second secondary heater, a secondary scrubber, a secondary compressor and a secondary discharge pump, wherein the secondary separator is provided with a secondary separation inlet, a salt leg, a secondary steam outlet, a secondary circulation outlet and a secondary circulation inlet, the salt leg is provided with a secondary separation outlet and a secondary discharge port, the primary separation outlet is communicated with the secondary separation inlet through the primary discharge pump, the secondary circulation outlet is communicated with the secondary separation outlet and is sequentially communicated with the secondary separation inlet through a first secondary heater, a secondary circulation pump and a second secondary heater, the secondary scrubber is provided with a secondary steam inlet and a secondary air outlet, the secondary steam outlet is communicated with the secondary steam inlet, and the secondary air outlet is communicated with the first secondary heater and the second secondary heater through the secondary compressor so as to pass through the secondary heater and the secondary heater; the secondary discharge port is communicated with the secondary circulation inlet through the secondary discharge pump;
The solid-liquid separation assembly is connected with the output end of the secondary discharge pump and is used for separating mother liquor and solids and conveying the mother liquor from which the solids are separated into a secondary separator;
the primary condensate water treatment assembly is connected with a heating medium outlet of the primary heater, and is used for carrying out preheating treatment on waste liquid before entering the primary heater and conveying condensate water into the primary scrubber;
and the secondary condensate water treatment assembly is used for carrying out steam heat exchange in the first secondary heater and the second secondary heater to form condensate water and conveying the condensate water into the secondary scrubber.
Preferably, in order to collect high-temperature condensed water formed by condensation when raw steam heats waste liquid, preheating the waste liquid before entering a heater by utilizing the high-temperature condensed water, conveying part of the condensed water into a gas washing tower, and carrying out gas washing treatment on secondary steam generated by a primary separator so that the secondary steam enters a primary compressor, wherein the primary condensed water treatment assembly comprises a primary condensed water tank, a primary condensed water pump, a first preheater, a second preheater, a third preheater, a steam-water separator and a vacuum pump, the steam-water separator is provided with a steam-water separation inlet, a steam-water separation outlet and a steam-water separation outlet, the input end of the primary condensed water pump is communicated with a heating medium outlet of the primary heater through the primary condensed water tank, and the output end of the primary condensed water pump is communicated with the heating medium inlet of the primary preheater; the heating medium outlet of the primary preheater is communicated with the outside, the material inlet is connected with a feed pump, and the material outlet is communicated with the material inlet of the second preheater; the heating medium inlet of the second preheater is communicated with the first-stage condensate water tank, the heating medium outlet is communicated with the steam-water separation inlet, and the material outlet is communicated with the material inlet of the third preheater; the material outlet of the third preheater is connected with the output end of the primary circulating pump, the heating medium inlet is used for connecting a raw steam source, and the heating medium outlet is communicated with the primary condensate water tank; the water outlet is communicated with the primary condensation water tank.
Preferably, in order to facilitate washing and purifying droplets contained in the secondary steam mixture of the primary separator, so that pure secondary steam enters the primary compressor, the primary condensate water treatment assembly further comprises a primary spray pump, wherein an input end of the primary spray pump is communicated with the primary condensate water tank, and an output end of the primary spray pump is communicated with the primary gas washing tower.
Preferably, in order to avoid the waste liquid to scale deposit in the pipe wall of primary separator and secondary separator in evaporation concentration process, influence heat transfer and increase the energy consumption of heating evaporation, simultaneously, eliminate the bubble in the waste liquid to heat transfer, save evaporation energy consumption, the material access connection of first pre-heater has waste liquid purification subassembly, waste liquid purification subassembly includes defoamer medical kit, defoamer medical pump, scale inhibitor medical kit and scale inhibitor medical pump, defoamer medical kit passes through defoamer medical pump with the material access intercommunication of first pre-heater, scale inhibitor medical kit passes through scale inhibitor medical pump with the material access intercommunication of first pre-heater.
Preferably, in order to collect the condensed water formed after the steam exchanges heat in the first secondary heater and the second secondary heater, the condensed water is utilized to spray in the secondary gas washing tower, liquid drops contained in the secondary steam generated by the secondary separator are washed and purified, the pure secondary steam enters the secondary compressor, the secondary condensed water treatment assembly comprises a secondary condensed water tank and a secondary condensed water pump, a first secondary condensed water outlet is arranged on the first secondary heater, a second secondary condensed water outlet is arranged on the second secondary heater, the first secondary condensed water outlet and the second secondary condensed water outlet are both communicated with the secondary condensed water tank, the input end of the secondary condensed water pump is communicated with the secondary condensed water tank, and the output end of the secondary condensed water pump is communicated with the heating medium inlet of the first preheater and the secondary gas washing tower.
Preferably, in order to separate solid and liquid in thick slurry, part of separated mother liquor is conveyed to a secondary separator for separation again, the solid-liquid separation assembly comprises a thickener, a centrifuge, a mother liquor tank and a mother liquor pump, the thickener is provided with a thick inlet, a slurry outlet and a clear liquor overflow port, the thick inlet is communicated with the output end of the secondary discharge pump, the slurry outlet is communicated with the mother liquor tank through the centrifuge, the clear liquor outlet is communicated with the mother liquor tank, and the mother liquor tank is communicated with the secondary separation inlet of the secondary separator through the mother liquor pump.
Preferably, the evaporation crystallization efficiency of the secondary evaporation crystallizer is improved in order to perform the hotter treatment of the waste liquid discharged from the evaporation concentrator as well. A fourth preheater is further arranged between the first-stage evaporation concentrator and the second-stage circulation evaporation crystallizer, a heating medium inlet of the fourth preheater is used for being connected with a raw steam source, a heating medium outlet is communicated with the second-stage condensation water tank, a material inlet is communicated with the output end of the first-stage discharge pump, and a material outlet is communicated with a second-stage separation inlet of the second-stage separator.
Preferably, in order to enhance the gas washing effect of the primary gas washing tower and the secondary gas washing tower, a primary gas washing inlet, a primary gas washing outlet and a primary water outlet are arranged on the primary gas washing tower, a primary reflux port is arranged on the primary separator, the primary gas washing outlet is communicated with the primary gas washing inlet through a primary gas washing pump, and the primary water outlet is communicated with the primary reflux port through a primary water outlet pump; the secondary gas washing tower is provided with a secondary gas washing inlet, a secondary gas washing outlet and a secondary water outlet, the secondary separator is provided with a secondary reflux port, the secondary gas washing outlet is communicated with the secondary gas washing inlet through a secondary gas washing pump, and the secondary water outlet is communicated with the secondary reflux port through a secondary water outlet pump.
Preferably, in order to facilitate conveying the condensate water remained in the first-stage gas washing tower into the first-stage condensate water tank, the first-stage gas outlet is connected with a first volute water pump through a first volute water tank, and the output end of the first volute water pump is communicated with the first-stage condensate water tank.
Preferably, in order to facilitate conveying the condensate water remained in the secondary scrubber to the primary condensate water tank, a primary compression water outlet is arranged on the primary compressor, the primary compression water outlet is connected with a second volute water pump through a second volute water tank, and the output end of the second volute water pump is communicated with the primary condensate water tank.
In summary, compared with the prior art, the garbage leachate two-stage MVR evaporative crystallizer sequentially carries out evaporative concentration and evaporative crystallization treatment on waste liquid through the first-stage evaporative concentrator and the second-stage circulating evaporative crystallizer, and the first-stage condensate water treatment assembly is used for collecting condensate water formed by condensing a heating medium and preheating the waste liquid while carrying out evaporative crystallization, and the second-stage condensate water treatment assembly is used for collecting condensate water formed by condensing the heating medium to carry out air washing while carrying out evaporative crystallization, so that the water consumption is greatly reduced, the operation cost is reduced, and the garbage leachate two-stage MVR evaporative crystallizer is more energy-saving and environment-friendly.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
FIG. 2 is a schematic diagram of a primary evaporative concentrator and primary condensate water treatment assembly of the present invention;
FIG. 3 is a schematic illustration of the treatment of waste stream material in a primary evaporative concentrator in accordance with the present invention;
FIG. 4 is a schematic illustration of the flow of steam in a primary evaporative concentrator according to the present invention;
FIG. 5 is a schematic illustration of the flow of condensate in a primary evaporative concentrator according to the present invention;
FIG. 6 is a schematic diagram of the structure of the two-stage circulation evaporative crystallizer, the two-stage condensate water treatment assembly and the solid-liquid separation assembly of the present invention;
FIG. 7 is a schematic diagram of the flow of the waste stream material of the present invention in a two-stage circulation evaporative crystallizer;
FIG. 8 is a schematic diagram of the flow of condensate in a two-stage circulation evaporative crystallizer according to the present invention;
FIG. 9 is a schematic diagram of the flow of steam in a two-stage circulation evaporative crystallizer according to the present invention;
FIG. 10 is a schematic view of the structure of the solid-liquid separation module of the present invention;
in the figure: 100. a primary separator; 101. a primary separation inlet; 102. a primary separation outlet; 103. a primary secondary steam outlet; 104. a primary return port; 200. a primary heater; 300. a primary circulation pump; 400. a primary discharge pump; 500. a primary scrubber; 501. a primary secondary steam inlet; 502. a first-stage air outlet; 503. a primary gas washing inlet; 504. a primary scrubbing outlet; 505. a primary water outlet; 600. a first stage compressor; 601. a primary compression inlet; 602. a first-stage compression air outlet; 603. a first-stage compression water outlet; 700. a secondary separator; 701. a secondary separation inlet; 702. a secondary separation outlet; 703. a secondary steam outlet; 704. a secondary reflux port; 705. salt legs; 706. a secondary circulation outlet; 707. a second-stage discharge port; 708. a secondary circulation inlet; 800. a secondary circulation pump; 900. a first secondary heater; 901. a first secondary heating inlet; 902. a first secondary heating outlet; 903. a first secondary raw steam inlet; 904. a first secondary heating steam inlet; 905. a first secondary condensate outlet; 906. a non-condensable gas outlet on the first second stage; 907. a non-condensable gas outlet under the first level two; 110. a second stage heater; 111. a second stage heating inlet; 112. a second stage heating outlet; 113. a second stage raw steam inlet; 114. a second stage heating steam inlet; 115. a second-stage condensate outlet; 116. a non-condensable gas outlet on the second stage; 117. a non-condensable gas outlet under the second stage; 118. a second level balancing interface; 120. a second-stage scrubber; 121. a secondary steam inlet; 122. a second-stage air outlet; 123. a secondary scrubbing inlet; 124. a secondary scrubbing outlet; 125. a secondary water outlet; 130. a secondary compressor; 140. a first-stage condensate water tank; 150. a primary condensate pump; 160. a first preheater; 170. a second preheater; 180. a third preheater; 190. a steam-water separator; 191. a steam-water separation inlet; 192. steam-water separation air outlet; 193. a steam-water separation water outlet; 210. a vacuum pump; 220. a feed pump; 230. a first stage spray pump; 240. a defoamer medicine box; 250. an antifoaming agent drug pump; 260. a scale inhibitor medicine box; 270. a scale inhibitor drug pump; 280. a second-stage condensate water tank; 290. a secondary condensate pump; 310. a thickener; 311. a thick inlet; 312. a slurry outlet; 313. a clear liquid overflow port; 320. a centrifuge; 321. a centrifugal inlet; 322. a centrifugal liquid outlet; 323. a centrifugal solids outlet; 330. a mother liquor tank; 340. a mother liquid pump; 350. a fourth preheater; 360. a primary air washing pump; 370. a first-stage water outlet pump; 380. a secondary air washing pump; 390. a secondary water outlet pump; 410. a first volute tank; 420. a first volute water pump; 430. a second volute tank; 440. a second volute water pump; 450. and a secondary discharge pump.
Detailed Description
The following describes the embodiments of the present invention further with reference to the drawings and examples. The following examples are only for more clearly illustrating the technical aspects of the present invention, and are not intended to limit the scope of the present invention.
As shown in fig. 1 to 10, the garbage leachate two-stage MVR evaporation crystallizer of the present invention comprises:
the primary evaporation concentrator comprises a primary separator 100, a primary heater 200, a primary circulating pump 300, a primary discharging pump 400, a primary scrubber 500 and a primary compressor 600, wherein the primary separator 100 is provided with a primary separation inlet 101, a primary separation outlet 102 and a primary secondary steam outlet 103, the primary separation outlet 102 is communicated with the primary separation inlet 101 through the primary circulating pump 300 and the primary heater 200 in sequence, the primary scrubber 500 is provided with a primary secondary steam inlet 501 and a primary air outlet 502, the primary secondary steam outlet 103 is communicated with the primary secondary steam inlet 501, the primary air outlet 502 is communicated with a heating medium inlet of the primary heater 200 through the primary compressor 600, and the heating medium inlet of the primary heater 200 is also used for connecting a raw steam source;
the secondary circulation evaporation crystallizer comprises a secondary separator 700, a secondary circulation pump 800, a first secondary heater 900, a second secondary heater 110, a secondary scrubber 120, a secondary compressor 130 and a secondary discharge pump 450, wherein the secondary separator 700 is provided with a secondary separation inlet 701, a salt leg 705, a secondary steam outlet 703, a secondary circulation outlet 706 and a secondary circulation inlet 708, the salt leg 705 is provided with a secondary separation outlet 702 and a secondary discharge outlet 707, the salt leg 705 is provided with a secondary separation outlet 702, the primary separation outlet 102 is communicated with the secondary separation inlet 701 through the primary discharge pump 400, the secondary circulation outlet 706 is communicated with the secondary separation outlet 702 and sequentially communicated with the secondary separation inlet 701 through the first secondary heater 900, the secondary circulation pump 800 and the second secondary heater 110, the secondary scrubber 120 is provided with a secondary steam inlet 121 and a secondary air outlet 122, the secondary steam outlet 703 is communicated with the secondary steam inlet 121, and the secondary air outlet 122 is communicated with the secondary heater 110 through the secondary compressor 130 and the secondary heater 110 through the secondary heater 900 and the secondary heater 110; the secondary discharge outlet 707 is communicated with a secondary circulation inlet 708 through a secondary discharge pump 450;
The solid-liquid separation component is connected with the output end of the secondary discharging pump 450 and is used for separating mother liquor and solids and conveying the mother liquor from which the solids are separated into the secondary separator 700;
the primary condensate water treatment assembly is connected with a heat medium outlet of the primary heater 200 to collect condensate water formed after the heat medium is condensed, and the condensate water is utilized to preheat waste liquid before entering the primary heater 200 and convey the condensate water into the primary scrubber 500;
the second-stage condensate water treatment assembly, the condensate water formed by the second-stage condensate water treatment assembly after steam heat exchange in the first second-stage heater 900 and the second-stage heater 110, and the condensate water is conveyed into the first-stage condensate water treatment assembly and the second-stage scrubber 120.
The garbage leachate two-stage MVR evaporation crystallizer is mainly used for evaporating, concentrating and crystallizing garbage leachate (hereinafter referred to as 'waste liquid'), when the device is operated, the waste liquid enters a first-stage evaporation concentrator for evaporating, concentrating and treating under the pushing action of a feed pump 220, the waste liquid firstly enters a first-stage heater 200 (the first-stage heater 200 is a plate heater), a heating medium is introduced into a heating medium inlet of the first-stage heater 200 while flowing in the first-stage heater 200, the heating medium is steam, namely the heating medium inlet is connected with a raw steam source, the waste liquid is heated through the raw steam, so that the waste liquid is conveyed into the first-stage separator 100 through the first-stage separation inlet 101 after being heated, and is heated in the first-stage separator 100 to achieve the aim of evaporating and concentrating; the waste liquid in the primary separator 100 is discharged from the separation outlet, enters the primary heater 200 again under the pushing action of the primary circulating pump 300, exchanges heat with the steam heating medium flowing in the primary heater 200, and enters the primary separator 100 after the temperature of the waste liquid is increased, and is circulated in such a way, so that the waste liquid is continuously evaporated and concentrated in the primary separator 100.
When the concentration of the waste liquid is raised to a certain concentration (the concentration can be actually set and controlled by an operator), the waste liquid is discharged from the primary separation outlet 102 and enters the secondary circulation evaporation crystallizer under the pushing action of the primary discharge pump 400.
The waste liquid firstly enters the secondary separator 700 through the secondary separation inlet 701, the waste liquid is discharged from the secondary separation outlet 702 while being evaporated and crystallized in the secondary separator 700, the waste liquid enters the first secondary heater 900, high-temperature steam is introduced into the first secondary heater 900, the steam exchanges heat with the waste liquid to achieve the effect of heating the waste liquid, then the waste liquid is discharged from the first secondary heater 900 and then enters the second secondary heater 110 through the secondary circulating pump 800, high-temperature steam is introduced into the second secondary heater 110, the steam exchanges heat with the waste liquid again, so that the effect of heating the waste liquid is achieved, after the waste liquid is heated, the waste liquid enters the secondary separator 700 from the secondary separation inlet 701, the waste liquid is continuously heated in the secondary separator 700 to boil and evaporate, the concentration of materials in the waste liquid is continuously increased, the separated crystals are deposited on the salt leg 705 at the bottom of the secondary separator 700, the secondary separation outlet 702 is arranged on the salt leg 705, and the secondary separation outlet 702 and the secondary circulation outlet 706 are mutually communicated, so that the crystals are prevented from blocking the bottom of the secondary separator 700. After the crystals are separated, the secondary discharge pump 450 is started, the crystal slurry with the crystals is discharged out of the secondary separator 700 under the pushing of the secondary discharge pump 450, part of crystal slurry returns to the secondary separator 700 from the secondary circulation inlet 708 again to continue evaporation crystallization, and the other part of crystal slurry enters into the solid-liquid separation assembly, the liquid (i.e. mother liquor) in the crystal slurry is separated from the solid (i.e. crystals) through the solid-liquid separation assembly, after separation, the mother liquor returns to the secondary separator 700 to continue evaporation crystallization, and the separated solid is discharged out of the system through incineration or landfill treatment.
In the above process, when the waste liquid passes through the primary evaporation concentrator, the waste liquid to be introduced into the primary separator 100 is heated in the primary heater 200, after the waste liquid is heated, the temperature of the steam is reduced, condensed water is formed by condensation, the temperature of the condensed water is higher than the initial temperature of the waste liquid, therefore, the system preheats the waste liquid before entering the primary separator 100 through the primary condensed water treatment component, thereby fully utilizing the heat of the condensed water, improving the temperature of the waste liquid entering the primary separator 100 and the primary heater 200, improving the evaporation concentration efficiency, simultaneously realizing energy saving, besides, when the waste liquid in the primary separator 100 is evaporated and concentrated, the produced secondary steam contains liquid drops, when the secondary steam mixed with the liquid drops enters the primary scrubber 500, the condensed water is conveyed into the primary scrubber 500 through the primary condensed water treatment component, and sprayed in the primary scrubber 500, thereby achieving the effect of scrubbing and purifying the liquid drops in the secondary steam, so that the pure secondary steam enters the compressor 600 for compression treatment, forming high-temperature steam, and conveying the high-temperature steam into the primary heater 200, thereby achieving the effect of heating the waste liquid, and reducing the consumption of the waste liquid.
When the waste liquid passes through the secondary circulation evaporation crystallizer, after the steam exchanges heat with the waste liquid in the first secondary heater 900 and the second secondary heater 110, the temperature is reduced to form condensed water, at the moment, after the formed condensed water is collected through the secondary condensed water treatment assembly, the collected condensed water is conveyed into the secondary scrubber 120, and the secondary steam mixed with liquid drops and generated by the secondary separator 700 and entering the secondary scrubber 120 is sprayed to separate the liquid drops from the secondary steam, so that the effect of scrubbing is achieved, the secondary steam after washing and purifying enters the secondary compressor 130, the secondary steam is compressed by the secondary compressor 130 to form high-temperature steam, and the waste liquid is heated in the first secondary heater 900 and the second secondary heater 110, so that the consumption of the generated steam is reduced, and the effect of saving energy and reducing the cost is achieved.
In a preferred embodiment, the primary condensate water treatment assembly comprises a primary condensate water tank 140, a primary condensate water pump 150, a first preheater 160, a second preheater 170, a third preheater 180, a steam-water separator 190 and a vacuum pump 210, wherein the steam-water separator 190 is provided with a steam-water separation inlet 191, a steam-water separation air outlet 192 and a steam-water separation water outlet 193, the input end of the primary condensate water pump 150 is communicated with the heating medium outlet of the primary heater 200 through the primary condensate water tank 140, and the output end is communicated with the heating medium inlet of the primary preheater; the heating medium outlet of the first-stage preheater is communicated with the outside, the material inlet is connected with a feed pump 220, and the material outlet is communicated with the material inlet of the second preheater 170; the heating medium inlet of the second preheater 170 is communicated with the first-stage condensate water tank 140, the heating medium outlet is communicated with the steam-water separation inlet 191, and the material outlet is communicated with the material inlet of the third preheater 180; the material outlet of the third preheater 180 is connected with the output end of the primary circulating pump 300, the heating medium inlet is used for connecting a raw steam source, and the heating medium outlet is communicated with the primary condensate water tank 140; the water outlet is communicated with the primary condensate tank 140.
The primary condensate water treatment assembly further includes a primary spray pump 230, the primary spray pump 230 having an input end in communication with the primary condensate water tank 140 and an output end in communication with the primary scrubber 500.
The material inlet of the first preheater 160 is connected with a waste liquid purifying component, and the waste liquid purifying component comprises a defoamer medicine box 240, a defoamer medicine pump 250, a scale inhibitor medicine box 260 and a scale inhibitor medicine pump 270, wherein the defoamer medicine box 240 is communicated with the material inlet of the first preheater 160 through the defoamer medicine pump 250, and the scale inhibitor medicine box 260 is communicated with the material inlet of the first preheater 160 through the scale inhibitor medicine pump 270.
The primary scrubber 500 is provided with a primary scrubber inlet 503, a primary scrubber outlet 504 and a primary water outlet 505, the primary separator 100 is provided with a primary return port 104, the primary scrubber outlet 504 is communicated with the primary scrubber inlet 503 through a primary scrubber pump 360, and the primary water outlet 505 is communicated with the primary return port 104 through a primary water outlet pump 370.
The first-stage water outlet 505 is connected with a first volute water pump 420 through a first volute water tank 410, and the output end of the first volute water pump 420 is communicated with the first-stage condensate water tank 140.
The primary compressor 600 is provided with a primary compression inlet 601, a primary compression air outlet 602 and a primary compression water outlet 603, the primary compression water outlet 603 is connected with a second volute water pump 440 through a second volute water tank 430, and the output end of the second volute water pump 440 is communicated with the primary condensation water tank 140.
Specifically, as shown in fig. 2-5, in the present invention, a primary separation inlet 101, a primary separation outlet 102, a primary secondary steam outlet 103, and a primary return 104 are provided on a primary separator 100. The primary separation inlet 101 is communicated with a material outlet of the primary heater 200, the primary separation outlet 102 is communicated with an input end of the primary circulating pump 300 and an input end of the primary discharging pump 400, the primary secondary steam outlet 103 is communicated with the primary scrubber 500, the primary return port 104 is connected with the primary water outlet pump 370, and the primary return port 104 is communicated with an output end of the primary water outlet pump 370.
The primary separation inlet 101 is used for introducing waste liquid to be evaporated and concentrated, the primary separation outlet 102 is used for discharging concentrated waste liquid, the primary secondary steam outlet 103 is used for discharging generated secondary steam during evaporation and concentration of the waste liquid, and the primary return port 104 is used for returning condensed water containing waste liquid with a certain concentration into the primary separator 100 again for evaporation and concentration treatment.
The primary scrubber 500 is provided with a primary secondary steam inlet 501, a primary air outlet 502, a primary scrubber inlet 503, a primary scrubber outlet 504 and a primary water outlet 505. The primary secondary steam inlet 501 is communicated with the primary secondary steam outlet 103, the primary air outlet 502 is communicated with the primary compression inlet 601 of the primary compressor 600, the primary scrubbing outlet 504 is communicated with the primary scrubbing outlet 504 through the primary scrubbing pump 360, the primary scrubbing outlet 504 is communicated with the output end of the primary spray pump 230, and the primary water outlet 505 is communicated with the primary return port 104 through the primary water outlet pump 370.
When the primary scrubber 500 operates, the primary secondary steam inlet 501 receives secondary steam with liquid drops discharged from the primary secondary steam outlet 103 of the primary separator 100, after the secondary steam is scrubbed, the scrubbed and purified secondary steam is discharged from the primary air outlet 502, part of waste liquid is contained in condensed water at the inner bottom of the primary scrubber 500, and after the waste liquid is discharged from the primary scrubbing outlet 504, the waste steam enters the primary scrubber 500 again from the primary scrubbing inlet 503 under the action of the primary scrubbing pump 360, the secondary steam mixed with the liquid drops is scrubbed, and when the concentration of the waste liquid in the condensed water in the primary scrubber 500 is raised to a certain degree, the condensed water is discharged from the primary water outlet 505, and returns to the primary separator 100 through the primary return port 104 under the action of the primary water outlet pump 370 to enter the evaporation concentration treatment.
When the primary evaporation concentrator of the device operates, raw steam is introduced into the primary heater 200 and exchanges heat with waste liquid to form condensed water, the condensed water enters the primary condensation water tank 140, the primary condensation water tank 140 contains condensed water and noncondensable gas, the initial temperature of the waste liquid, the temperature of the condensed water, the noncondensable gas and the temperature of the raw steam are sequentially increased, therefore, the waste liquid is sequentially preheated by utilizing the condensed water, the noncondensable gas and the raw steam respectively before entering the primary heater 200 through the temperature difference of the four components, the waste liquid can have higher temperature before entering the primary heater 200 through three times of preheating, so that the effect of quickly heating the waste liquid is achieved, and meanwhile, the heat of the raw steam is reasonably utilized to perform multiple times of preheating, thereby achieving the purposes of energy conservation and consumption reduction.
Specifically, the condensed water is introduced into the heat medium inlet of the first preheater 160 from the first stage condensate water tank 140 under the action of the first stage condensate water pump 150, flows in the first preheater 160, and performs the first preheating on the waste liquid, so that after the temperature of the waste liquid is raised, the waste liquid is discharged from the heat medium outlet of the first preheater 160 to perform the biochemical removal treatment.
After being discharged from the material outlet of the first preheater 160, the waste liquid enters the second preheater 170 through the material inlet of the second preheater 170, noncondensable gas in the first-stage condensate water tank 140 enters the second preheater 170 from the heat medium inlet of the second preheater 170 and exchanges heat with the waste liquid, so that after the temperature of the waste liquid rises, the waste liquid is discharged from the material outlet of the second preheater 170, the noncondensable gas after heat exchange enters the steam-water separator 190 through the steam-water separation inlet 191, gas-liquid separation is performed in the steam-water separator 190, air is discharged from the steam-water separation air outlet 192, the separated moisture forms condensed water after being discharged from the system for tail gas removal treatment under the action of the vacuum pump 210, and the condensed water enters the first-stage condensate water tank 140.
Waste liquid after heat exchange with noncondensable gas enters the third preheater 180 from a material inlet of the third preheater 180, raw steam enters the third preheater 180 through a heating medium inlet of the third preheater 180, and the raw steam and the waste liquid are subjected to heat exchange, so that after the waste liquid is heated, the waste liquid enters the primary heater 200 from a material outlet, the temperature of the raw steam after heat exchange is reduced, and the waste liquid is condensed into condensed water and enters the primary condensate water tank 140.
The waste liquid purification component is further arranged at the material inlet of the first preheater 160, when the waste liquid purification component is operated, the defoamer in the defoamer medicine tank 240 is conveyed into the waste liquid by the defoamer medicine pump 250 while the waste liquid is introduced into the first preheater 160, so that air bubbles in the waste liquid are eliminated, the heat exchange effect of the waste liquid, condensed water, noncondensable gas and raw steam is prevented from being influenced by the bubbles in the waste liquid, the scale inhibitor in the scale inhibitor medicine tank 260 is conveyed into the waste liquid by the scale inhibitor medicine pump 270, scaling on the pipe wall of a pipeline and the inner walls of the primary separator 100 and the secondary separator 700 after the waste liquid is prevented from evaporating is avoided, the heat absorption of the waste liquid is prevented, and the energy consumption required for evaporating the waste liquid is increased.
The waste liquid evaporates in the first-stage separator 100 to generate secondary steam, partial liquid drops are mixed with the secondary steam, the secondary steam is discharged from the first-stage secondary steam outlet 103 and enters the first-stage gas washing tower 500 through the first-stage secondary steam inlet 501, meanwhile, the first-stage spray pump 230 is started to pump condensed water in the first-stage condensate water tank 140, the condensed water enters the first-stage gas washing tower 500 through the first-stage gas washing inlet 503 to spray, the liquid drops in the secondary steam are washed and purified, the condensed water absorbs the liquid drops in the secondary steam and then contains oily waste liquid, the first-stage gas washing pump 360 is started, the condensed water discharged from the first-stage gas washing outlet 504 is conveyed into the first-stage gas washing tower 500 again through the first-stage gas washing inlet 503 to spray so as to achieve washing and purifying of the secondary steam liquid drops, after the concentration of the condensed water waste liquid in the first-stage gas washing tower 500 is increased to a certain extent, the first-stage water outlet pump 370 is started to convey the condensed water discharged from the first-stage water outlet 505 into the first-stage separator 100 through the first-stage return port 104, and the condensed water containing waste water is evaporated and concentrated in the first-stage separator 100.
After washing and purifying, the secondary steam in the primary scrubber 500 is discharged through the primary air outlet 502, enters the primary compressor 600 through the primary compression inlet 601, performs compression work on the secondary steam by the primary compressor 600, improves the pressure and temperature of the secondary steam, forms heating steam, enters the primary heater 200 after being discharged from the primary compression air outlet 602, exchanges heat with waste liquid materials to be introduced into the primary separator 100 after flowing in the primary heater 200, enables the waste liquid to be introduced into the primary separator 100 after temperature rise, and forms condensed water after heat exchange, and enters the primary condensed water tank 140. By adopting the mode, compression work is performed by utilizing the generated secondary steam to form heating steam capable of exchanging heat with the waste liquid, so that continuous introduction of raw steam into the primary heater 200 is avoided, the consumption of the raw steam is reduced, the energy-saving and cost-reducing effects are achieved, and meanwhile, the efficiency of rapid evaporation and concentration of the waste liquid in the primary separator 100 is improved.
The primary scrubber 500 washes and purifies the secondary steam and the liquid droplets, and at the same time, condensed water in the primary scrubber 500 enters the first volute water tank 410, the first volute water pump 420 is started, and the condensed water in the first volute water tank 410 is extracted and conveyed into the primary condensed water tank 140.
And the first-stage compressor 600 produces condensed water after compressing the secondary steam, the condensed water is discharged from the first-stage compression water outlet 603 and enters the second volute water tank 430, the second volute water pump 440 is started, and the condensed water in the second volute water tank 430 is extracted and conveyed into the first-stage condensed water tank 140.
After the mode is adopted, condensed water is formed by utilizing secondary steam heat exchange generated by heat exchange of raw steam and evaporation of waste liquid, so that cooling water is not required to be additionally added in the use process of the device, the water consumption is reduced, and the operation cost of the device is reduced.
In a preferred embodiment, a fourth preheater 350 is further disposed between the primary evaporative concentrator and the secondary circulating evaporative crystallizer, a heating medium inlet of the fourth preheater 350 is used for connecting a raw steam source, a heating medium outlet is communicated with the secondary condensate water tank 280, a material inlet is communicated with an output end of the primary discharge pump 400, and a material outlet is communicated with a secondary separation inlet 701 of the secondary separator 700.
After the waste liquid is evaporated and concentrated by the evaporation concentrator, the generated high-temperature concentrated waste liquid enters the fourth preheater 350 from the material inlet of the fourth preheater 350 under the pushing action of the first-stage discharge pump 400, meanwhile, the raw steam source conveys the raw steam with higher temperature into the fourth preheater 350 through the heating medium inlet of the fourth preheater 350, after the raw steam exchanges heat with the concentrated waste liquid, the concentrated waste liquid enters the second-stage separator 700 through the second-stage separation inlet 701 for evaporation and crystallization treatment, the temperature of the raw steam after the heat exchange is reduced, and the condensed water is formed after the condensed water enters the second-stage condensation water tank 280.
As shown in fig. 6 to 9, a salt leg 705 is provided at the bottom of the secondary separator 700, a secondary separation outlet 702 and a secondary discharge outlet 707 are provided on the salt leg 705, and a secondary separation inlet 701, a secondary steam outlet 703, a secondary return 704, a secondary circulation outlet 706 and a secondary circulation inlet 708 are provided on the secondary separator 700. The secondary separation inlet 701 is communicated with the material outlet of the fourth preheater 350, the secondary separation outlet 702 is communicated with the first secondary heater 900, the secondary steam outlet 703 is communicated with the secondary steam inlet 121, the secondary reflux port 704 is connected with the secondary water outlet pump 390, the secondary reflux port 704 is communicated with the output end of the secondary water outlet pump 390, the secondary circulation outlet 706 is communicated with the secondary separation outlet 702, and the secondary discharge outlet 707 is communicated with the secondary circulation inlet 708 through the secondary discharge pump 450.
Wherein, the secondary separation inlet 701 is used for introducing the waste liquid to be evaporated and crystallized after concentration, and the secondary steam outlet 703 is convenient for discharging secondary steam when the waste liquid is evaporated and crystallized; the secondary reflux port 704 is used for introducing condensed water containing waste liquid with a certain concentration; during evaporative crystallization, crystals are precipitated from the concentrated waste liquid, the crystals are settled on a salt leg 705 at the bottom of the secondary separator 700, the secondary separation outlet 702 is communicated with a secondary discharge outlet 707 to prevent the crystals from being blocked due to the deposition on the bottom of the salt leg 705, and the concentrated waste liquid enters the secondary separator 700 through a secondary separation inlet 701 for evaporative crystallization through heating treatment after being discharged from a secondary circulation outlet 706; the secondary discharge outlet 707 is used for discharging the waste liquid mixed with solids, namely slurry containing precipitated crystals; the slurry mixed with crystals is conveniently re-conveyed into the secondary separator 700 through the secondary recycle inlet 708 for repeated evaporative crystallization.
The first secondary heater 900 is provided with a first secondary heating inlet 901, a first secondary heating outlet 902, a first secondary raw steam inlet 903, a first secondary heating steam inlet 904, a first secondary condensed water outlet 905, a first secondary upper noncondensable gas outlet 906 and a first secondary lower noncondensable gas outlet 907; the second-stage heater 110 is provided with a second-stage heating inlet 111, a second-stage heating outlet 112, a second-stage raw steam inlet 113, a second-stage heating steam inlet 114, a second-stage condensed water outlet 115, a second-stage upper noncondensable gas outlet 116, a second-stage lower noncondensable gas outlet 117 and a second-stage balance interface 118.
Wherein, the first secondary heating inlet 901 is communicated with the secondary circulation outlet 706 and the secondary separation outlet 702, the first secondary heating outlet 902 is communicated with the second secondary heating inlet 111 through the secondary circulation pump 800, the second secondary heating outlet 112 is communicated with the secondary separation inlet 701, the first secondary raw steam inlet 903 and the second secondary raw steam inlet 113 are both connected with a raw steam source, the first secondary heating steam inlet 904 and the second secondary heating steam inlet 114 are both connected with the output end of the secondary compressor 130, the first secondary condensed water outlet 905 and the second secondary condensed water outlet 115 are both communicated with the secondary condensed water tank 280, and the first secondary upper non-condensable gas outlet 906, the second secondary lower non-condensable gas outlet 117, the second upper non-condensable gas outlet 116 and the second lower non-condensable gas outlet 117 are all communicated with the outside; the second stage balancing interface 118 communicates with a second stage condensate water tank 280.
When the first secondary heater 900 operates, raw steam and heating steam enter the first secondary heater 900 through the first secondary raw steam inlet 903 and the first secondary heating steam inlet 904 respectively, waste liquid to be evaporated and crystallized enters the first secondary heater 900 from the first secondary heating inlet 901, waste liquid with lower temperature exchanges heat with raw steam and heating steam with higher temperature, so that after the temperature of the waste liquid rises, the waste liquid is discharged from the first secondary heating outlet 902, the temperature of the raw steam and the heating steam is reduced after heat exchange, condensed water and noncondensable gas are formed, the condensed water is discharged from the first secondary condensed water outlet 905, and the noncondensable gas is discharged to the outside from the first secondary noncondensable gas outlet 906 and the first secondary noncondensable gas outlet 907 for tail gas removal treatment.
When the second-stage heater 110 operates, raw steam and heating steam enter the second-stage heater 110 through a second-stage raw steam inlet 113 and a second-stage heating steam inlet 114 respectively, waste liquid to be evaporated and crystallized enters the second-stage heater 110 from the second-stage heating inlet 111, waste liquid with lower temperature exchanges heat with raw steam and heating steam with higher temperature, so that after the temperature of the waste liquid rises, the waste steam is discharged from a second-stage heating outlet 112, the temperature of the raw steam and the heating steam is reduced after heat exchange, condensed water and noncondensable gas are formed, the condensed water is discharged from a second-stage condensed water outlet 115, and noncondensable gas is discharged from a second-stage upper noncondensable gas outlet 116 and a second-stage lower noncondensable gas outlet 117; the second stage balancing interface 118 is used to maintain pressure balance within the second stage heater 110.
The secondary scrubber 120 is provided with a secondary steam inlet 121, a secondary air outlet 122, a secondary scrubber inlet 123, a secondary scrubber outlet 124 and a secondary water outlet 125. The secondary steam inlet 121 is communicated with a secondary steam outlet 703, the secondary air outlet 122 is connected with the input end of the secondary compressor 130, the secondary scrubbing outlet 124 is communicated with a secondary scrubbing inlet 123 through a secondary scrubbing pump 380, the secondary scrubbing inlet 123 is connected with the output end of the secondary condensate pump 290, and the secondary water outlet 125 is communicated with a secondary return port 704 through a secondary water outlet pump 390. The secondary steam inlet 121 is used for introducing secondary steam mixed with liquid drops generated by the evaporation and crystallization of the waste liquid into the secondary scrubber 120 when the secondary separator 700 is operated, the secondary air outlet 122 is used for discharging the secondary steam after gas scrubbing, so that the secondary steam enters the secondary compressor 130 and forms heating steam in a compression work mode, the secondary scrubber inlet 123 is used for introducing condensed water into the secondary scrubber 120 to scrub and purify the secondary steam, and the secondary scrubber outlet 124 is used for discharging the condensed water after gas scrubbing; in the gas washing process, the condensed water is contacted with the secondary steam, so that the condensed water contains waste liquid components, and the concentration of the waste liquid is increased along with the gas washing, and at the moment, the condensed water with higher concentration of the waste liquid is conveniently discharged through the secondary water outlet 125, so that the condensed water is conveyed into the secondary separator 700 through the secondary reflux port 704, and the evaporation and crystallization treatment is continuously carried out.
The secondary condensate water treatment assembly comprises a secondary condensate water tank 280 and a secondary condensate water pump 290, wherein a first secondary condensate water outlet 905 and a second secondary condensate water outlet 115 are both communicated with the secondary condensate water tank 280, the input end of the secondary condensate water pump 290 is communicated with the secondary condensate water tank 280, and the output end is communicated with the heating medium inlet of the first preheater 160 and the secondary scrubbing inlet 123 of the secondary scrubbing tower 120; the second stage balancing interface 118 communicates with a second stage condensate water tank 280.
In the operation of the secondary circulation evaporation crystallizer, waste liquid preheated by the fourth preheater 350 enters the secondary separator 700 through the secondary separation inlet 701, evaporated and crystallized in the secondary separator 700, precipitated crystals are deposited on the salt legs 705 at the bottom, concentrated waste liquid is sequentially discharged from the secondary circulation outlet 706, enters the first secondary heater 900 through the first secondary heating inlet 901 and then is discharged from the first secondary heating outlet 902, enters the second secondary heater 110 through the second secondary heating inlet 111 under the pushing action of the secondary circulation pump 800 and then is discharged from the second secondary heating outlet 112, enters the secondary separator 700 through the secondary separation inlet 701, and circularly flows in such a way that a raw steam source leads raw steam into the first secondary heater 900 and the second secondary heater 110 through the first secondary steam inlet 903 and the second secondary raw steam inlet 113 respectively in the circulation flow process, after the temperature of the waste liquid in the system is increased to a set value, a first secondary steam inlet 903 of a first secondary heater 900 and a second secondary steam inlet 113 of a second secondary heater 110 are closed, a secondary compressor 130 is started, after the secondary steam generated during the previous evaporation and crystallization of the waste liquid in the secondary separator 700 is washed and purified by a secondary gas washing tower 120 and gas-liquid separated, pure secondary steam is introduced into the secondary compressor 130, the secondary steam is compressed and acted by the secondary compressor 130, the temperature and the pressure of the secondary steam are increased to form heating steam, the heating steam enters the first secondary heater 900 and the second secondary heater 110 through a first secondary heating steam inlet 904 and a second secondary heating steam inlet 114 respectively, the heating steam exchanges heat with the circulating waste liquid, the waste liquid in the system is continuously boiled, after the raw steam and the heating steam are condensed, condensed water and non-condensed gas are formed, the condensed water is discharged from a first secondary condensed water outlet 905 and a second secondary condensed water outlet 115 and enters into a secondary condensed water tank 280, condensed water in the secondary condensed water tank 280 is pumped by a secondary condensed water pump 290 and is conveyed into the first preheater 160 through a heating medium inlet of the first preheater 160 so as to exchange heat with the waste liquid before entering the first separator 100, and then the condensed water is discharged out for biochemical treatment, and a second secondary balance interface 118 is communicated with the secondary condensed water tank 280 so that the condensed water in the second secondary heater 110 can smoothly flow into the secondary condensed water tank 280; the noncondensable gases are respectively discharged from the first-stage noncondensable gas outlet 906, the first-stage noncondensable gas outlet 907, the second-stage noncondensable gas outlet 116 and the second-stage noncondensable gas outlet 117, and then are collected, and the tail gas is treated by a discharge system. The waste liquid is saturated and crystallized in the salt leg 705, and at this time, the secondary discharging pump 450 is started to convey the crystals and the mother liquid to the solid-liquid separation component for solid-liquid separation treatment.
In the operation process of the secondary separator 700, secondary steam is generated by boiling internal waste liquid, secondary steam inclusion liquid drops are discharged from a secondary steam outlet 703 and then enter the secondary scrubbing tower 120 through a secondary steam inlet 121, condensed water in a secondary condensed water tank 280 is pumped by a secondary condensed water pump 290 and is conveyed into the secondary scrubbing tower 120 through a secondary scrubbing inlet 123 for spraying so as to achieve the effect of washing purification and gas-liquid separation of the secondary steam, after scrubbing, condensed water is deposited in the secondary scrubbing tower 120, at the moment, the condensed water in the secondary condensed water tank 280 is not required to be pumped by the secondary condensed water pump 290, and is pumped from a secondary scrubbing outlet 124 instead by a secondary scrubbing pump 380 and is conveyed into the secondary scrubbing tower 120 through the secondary scrubbing inlet 123 for continuous spraying scrubbing treatment.
In the gas washing process, pure secondary steam is formed, the secondary steam is discharged from the secondary gas outlet 122 and then enters the secondary compressor 130, compression work is performed by the secondary compressor 130, so that heating steam is formed after the temperature and the pressure of the steam are increased, and waste liquid circularly flowing in the first secondary heater 900 and the second secondary heater 110 is heated.
As the scrubbing proceeds, the concentration of the waste liquid in the condensed water deposited in the secondary scrubber 120 gradually increases, and when the concentration increases to a set value, the condensed water with higher concentration in the secondary scrubber 120 is pumped by the secondary water outlet pump 390 through the secondary water outlet 125 and is conveyed to the secondary return port 704, so that the condensed water enters the secondary separator 700 for evaporation crystallization treatment.
As crystals are deposited inside the salt leg 705, the concentration of the mother liquor increases continuously, and the mixture of crystals and mother liquor is sent to a solid-liquid separation assembly for separation treatment by a secondary discharge pump 450.
As shown in fig. 10, the solid-liquid separation assembly comprises a thickener 310, a centrifuge 320, a mother liquor tank 330 and a mother liquor pump 340, wherein the thickener 310 is provided with a thickener inlet 311, a slurry outlet 312 and a clear liquid overflow port 313, the thickener inlet 311 is communicated with the output end of the secondary discharge pump, the slurry outlet 312 is communicated with the mother liquor tank 330 through the centrifuge 320, the clear liquid outlet is communicated with the mother liquor tank 330, and the mother liquor tank 330 is communicated with the secondary separation inlet 701 of the secondary separator 700 through the mother liquor pump 340.
Specifically, a thick inlet 311 is arranged at the top of the thickener 310, a clear liquid overflow port 313 is arranged on the side wall, and a slurry outlet 312 is arranged at the bottom; the centrifuge 320 is provided with a centrifugal inlet 321, a centrifugal liquid outlet 322 and a centrifugal solid outlet 323; the thick inlet 311 is connected with the output end of the secondary discharging pump 450, the clear liquid overflow port 313 is communicated with the mother liquor tank 330, the slurry outlet 312 is communicated with the centrifugal inlet 321, the centrifugal solid outlet 323 is communicated with the outside, the centrifugal liquid outlet 322 is communicated with the mother liquor tank 330, and the output end of the mother liquor pump 340 is communicated with the second secondary heating inlet 111.
When the solid-liquid separation assembly is operated, the discharging pump 450 conveys the mixture of the crystals and the mother liquor into the thickener 310 through the thickener inlet 311, the crystals of the solid particles settle at the bottom of the thickener 310 in the thickener 310, so that the liquid level of the clear liquid in the thickener 310 is gradually increased, the clear liquid overflows from the clear liquid overflow port 313 along with the gradual increase of the liquid level and enters the mother liquor tank 330, the slurry mixture formed by mixing the crystals and part of the mother liquor is discharged from the slurry outlet 312 at the bottom and then enters the centrifuge 320 through the centrifugal inlet 321, the solid-liquid separation is carried out on the slurry through the centrifuge 320, the centrifugal solid is subjected to the slurry removal drying, the dried centrifugal solid is discharged to the outside through the centrifugal solid outlet 323 for the landfill removal or the incineration innocent treatment, and the separated mother liquor flows into the mother liquor tank 330 from the centrifugal liquid outlet 322. The mother liquid pump 340 pumps the mother liquid in the mother liquid tank 330, the mother liquid is divided into two parts for treatment, wherein one part of the mother liquid is conveyed to the second-stage heating inlet 111 through the mother liquid pump 340, so that after the part of the mother liquid is subjected to heating treatment through the second-stage heater 110, the mother liquid returns to the second-stage separator 700 for continuous evaporation and crystallization, and the other part of the mother liquid is conveyed to an external paddle dryer through the mother liquid pump 340 for drying treatment, so that solidification is realized, and the solidified dry solid adopts a landfill or incineration harmless treatment mode.
The foregoing is merely a preferred embodiment of the present invention, and it should be noted that it will be apparent to those skilled in the art that several modifications and variations can be made without departing from the technical principle of the present invention, and these modifications and variations should also be regarded as the scope of the invention.

Claims (10)

1. A landfill leachate doublestage MVR evaporation crystallizer, characterized in that includes:
the primary evaporation concentrator comprises a primary separator (100), a primary heater (200), a primary circulating pump (300), a primary discharge pump (400), a primary scrubbing tower (500) and a primary compressor (600), wherein the primary separator (100) is provided with a primary separation inlet (101), a primary separation outlet (102) and a primary secondary steam outlet (103), the primary separation outlet (102) is communicated with the primary separation inlet (101) sequentially through the primary circulating pump (300) and the primary heater (200), the primary scrubbing tower (500) is provided with a primary secondary steam inlet (501) and a primary air outlet (502), the primary secondary steam outlet (103) is communicated with the primary secondary steam inlet (501), the primary air outlet (502) is communicated with a heating medium inlet of the primary heater (200) through the primary compressor (600), and the heating medium inlet of the primary heater (200) is also used for being connected with a raw steam source;
A secondary circulation evaporation crystallizer, the secondary circulation evaporation crystallizer comprises a secondary separator (700), a secondary circulation pump (800), a first secondary heater (900), a second secondary heater (110), a secondary scrubber tower (120), a secondary compressor (130) and a secondary discharge pump (450), the secondary separator (700) is provided with a secondary separation inlet (701), a salt leg (705), a secondary steam outlet (703), a secondary circulation outlet (706) and a secondary circulation inlet (708), the salt leg (705) is provided with a secondary separation outlet (702) and a secondary discharge port (707), the primary separation outlet (102) is communicated with the secondary separation inlet (701) through the primary discharge pump (400), the secondary circulation outlet (706) is communicated with the secondary separation outlet (702) and is sequentially communicated with the first secondary heater (900), the secondary circulation pump (800) and the second secondary heater (110) through the secondary separation inlet (701), the secondary separation outlet (121) is communicated with the secondary scrubber tower (121), the secondary air outlet (122) is communicated with the first secondary heater (900) and the second secondary heater (110) through the secondary compressor (130) to heat waste liquid passing through the first secondary heater (900) and the second secondary heater (110); the secondary discharge port (707) is communicated with the secondary circulation inlet (708) through the secondary discharge pump (450);
The solid-liquid separation assembly is connected with the output end of the secondary discharge pump and is used for separating mother liquor and solids and conveying the mother liquor from which the solids are separated into a secondary separator (700);
the primary condensate water treatment assembly is connected with a heat medium outlet of the primary heater (200) to collect condensate water formed after the heat medium is condensed, and the condensate water is utilized to preheat waste liquid before entering the primary heater (200) and convey the condensate water into the primary scrubber (500);
and the secondary condensate water treatment assembly is used for carrying out steam heat exchange in the first secondary heater (900) and the second secondary heater (110) to form condensate water and conveying the condensate water into the secondary scrubber (120).
2. The landfill leachate double-stage MVR evaporation crystallizer according to claim 1, characterized in that: the primary condensate water treatment assembly comprises a primary condensate water tank (140), a primary condensate water pump (150), a first preheater (160), a second preheater (170), a third preheater (180), a steam-water separator (190) and a vacuum pump (210), wherein the steam-water separator (190) is provided with a steam-water separation inlet (191), a steam-water separation air outlet (192) and a steam-water separation water outlet (193), the input end of the primary condensate water pump (150) is communicated with the heating medium outlet of the primary heater (200) through the primary condensate water tank (140), and the output end of the primary condensate water pump is communicated with the heating medium inlet of the primary preheater; the heating medium outlet of the primary preheater is communicated with the outside, the material inlet is connected with a feed pump (220), and the material outlet is communicated with the material inlet of the second preheater (170); the heating medium inlet of the second preheater (170) is communicated with the first-stage condensation water tank (140), the heating medium outlet is communicated with the steam-water separation inlet (191), and the material outlet is communicated with the material inlet of the third preheater (180); the material outlet of the third preheater (180) is connected with the output end of the primary circulating pump (300), the heating medium inlet is used for connecting a raw steam source, and the heating medium outlet is communicated with the primary condensing water tank (140); the water outlet is communicated with the primary condensation water tank (140).
3. The landfill leachate double-stage MVR evaporation crystallizer according to claim 2, characterized in that: the primary condensate water treatment assembly further comprises a primary spray pump (230), the input end of the primary spray pump (230) is communicated with the primary condensate water tank (140), and the output end of the primary spray pump is communicated with the primary gas washing tower (500).
4. The landfill leachate double-stage MVR evaporation crystallizer according to claim 2, characterized in that: the material inlet of first pre-heater (160) is connected with waste liquid purification subassembly, waste liquid purification subassembly includes defoaming agent medical kit (240), defoaming agent medical kit (250), scale inhibitor medical kit (260) and scale inhibitor medical kit (270), defoaming agent medical kit (240) pass through defoaming agent medical kit (250) with the material inlet intercommunication of first pre-heater (160), scale inhibitor medical kit (260) pass through scale inhibitor medical kit (270) with the material inlet intercommunication of first pre-heater (160).
5. The landfill leachate double-stage MVR evaporation crystallizer according to claim 1, characterized in that: the secondary condensate water treatment assembly comprises a secondary condensate water tank (280) and a secondary condensate water pump (290), a first secondary condensate water outlet (905) is formed in the first secondary heater (900), a second secondary condensate water outlet (115) is formed in the second secondary heater (110), the first secondary condensate water outlet (905) and the second secondary condensate water outlet (115) are communicated with the secondary condensate water tank (280), the input end of the secondary condensate water pump (290) is communicated with the secondary condensate water tank (280), and the output end of the secondary condensate water pump is communicated with the heat medium inlet of the first preheater (160) and the secondary scrubber (120).
6. The landfill leachate double-stage MVR evaporation crystallizer according to claim 1, characterized in that: the solid-liquid separation assembly comprises a thickener (310), a centrifugal machine (320), a mother liquor tank (330) and a mother liquor pump (340), wherein a thickener inlet (311), a slurry outlet (312) and a clear liquid overflow port (313) are formed in the thickener (310), the thickener inlet (311) is communicated with the output end of the secondary discharge pump, the slurry outlet (312) is communicated with the mother liquor tank (330) through the centrifugal machine (320), the clear liquid outlet is communicated with the mother liquor tank (330), and the mother liquor tank (330) is communicated with a secondary separation inlet (701) of the secondary separator (700) through the mother liquor pump (340).
7. The landfill leachate double-stage MVR evaporation crystallizer according to claim 5, characterized in that: a fourth preheater (350) is further arranged between the first-stage evaporation concentrator and the second-stage circulation evaporation crystallizer, a heating medium inlet of the fourth preheater (350) is used for being connected with a raw steam source, a heating medium outlet is communicated with the second-stage condensation water tank (280), a material inlet is communicated with the output end of the first-stage discharge pump (400), and a material outlet is communicated with a second-stage separation inlet (701) of the second-stage separator (700).
8. The landfill leachate double-stage MVR evaporation crystallizer according to claim 1, characterized in that: the primary gas washing tower (500) is provided with a primary gas washing inlet (503), a primary gas washing outlet (504) and a primary water outlet (505), the primary separator (100) is provided with a primary reflux port (104), the primary gas washing outlet (504) is communicated with the primary gas washing inlet (503) through a primary gas washing pump (360), and the primary water outlet (505) is communicated with the primary reflux port (104) through a primary water outlet pump (370); the secondary gas washing tower (120) is provided with a secondary gas washing inlet (123), a secondary gas washing outlet (124) and a secondary water outlet (125), the secondary separator (700) is provided with a secondary reflux port (704), the secondary gas washing outlet (124) is communicated with the secondary gas washing inlet (123) through a secondary gas washing pump (380), and the secondary water outlet (125) is communicated with the secondary reflux port (704) through a secondary water outlet pump (390).
9. The landfill leachate double-stage MVR evaporation crystallizer according to claim 8, characterized in that: the first-stage air outlet (502) is connected with a first volute water pump (420) through a first volute water tank (410), and the output end of the first volute water pump (420) is communicated with the first-stage condensation water tank (140).
10. The landfill leachate double-stage MVR evaporation crystallizer according to claim 2, characterized in that: the primary compressor (600) is provided with a primary compression water outlet (603), the primary compression water outlet (603) is connected with a second volute water pump (440) through a second volute water tank (430), and the output end of the second volute water pump (440) is communicated with the primary condensation water tank (140).
CN202211671610.5A 2022-12-26 2022-12-26 Garbage leachate doublestage MVR evaporation crystallizer Pending CN116081741A (en)

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN202744414U (en) * 2012-08-16 2013-02-20 广州新普利节能环保科技有限公司 Rare metal waste water zero discharge device
CN104803535A (en) * 2015-05-06 2015-07-29 广州新普利节能环保科技有限公司 Recycling system and recycling process for recycling salt from desulfurization waste water
CN105402999A (en) * 2015-12-25 2016-03-16 孙发喜 Mechanical steam recompression type vacuum tube bundle drying system
CN211987181U (en) * 2020-03-17 2020-11-24 河北乐恒节能设备有限公司 System for producing lithium hydroxide monohydrate by applying MVR technology and cooling crystallization technology
CN214004100U (en) * 2020-08-31 2021-08-20 广东闻扬环境科技有限公司 Contain salt effluent treatment plant
CN215781562U (en) * 2021-10-12 2022-02-11 江苏迈安德节能蒸发设备有限公司 Low-density organic salt low-temperature evaporation crystallization separation system
CN216549700U (en) * 2021-12-01 2022-05-17 江阴市江中设备制造有限公司 Potassium perchlorate effluent evaporation plant
CN216997745U (en) * 2022-04-07 2022-07-19 中洁蓝环保科技有限公司 Salt system is divided in industrial waste water salt washing

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN202744414U (en) * 2012-08-16 2013-02-20 广州新普利节能环保科技有限公司 Rare metal waste water zero discharge device
CN104803535A (en) * 2015-05-06 2015-07-29 广州新普利节能环保科技有限公司 Recycling system and recycling process for recycling salt from desulfurization waste water
CN105402999A (en) * 2015-12-25 2016-03-16 孙发喜 Mechanical steam recompression type vacuum tube bundle drying system
CN211987181U (en) * 2020-03-17 2020-11-24 河北乐恒节能设备有限公司 System for producing lithium hydroxide monohydrate by applying MVR technology and cooling crystallization technology
CN214004100U (en) * 2020-08-31 2021-08-20 广东闻扬环境科技有限公司 Contain salt effluent treatment plant
CN215781562U (en) * 2021-10-12 2022-02-11 江苏迈安德节能蒸发设备有限公司 Low-density organic salt low-temperature evaporation crystallization separation system
CN216549700U (en) * 2021-12-01 2022-05-17 江阴市江中设备制造有限公司 Potassium perchlorate effluent evaporation plant
CN216997745U (en) * 2022-04-07 2022-07-19 中洁蓝环保科技有限公司 Salt system is divided in industrial waste water salt washing

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