CN105836951B - A kind of electroplating waste processing process and device - Google Patents
A kind of electroplating waste processing process and device Download PDFInfo
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- CN105836951B CN105836951B CN201610346264.1A CN201610346264A CN105836951B CN 105836951 B CN105836951 B CN 105836951B CN 201610346264 A CN201610346264 A CN 201610346264A CN 105836951 B CN105836951 B CN 105836951B
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- heat exchanger
- separator
- falling film
- pump
- forced circulation
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- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000002699 waste material Substances 0.000 title claims abstract description 19
- 238000009713 electroplating Methods 0.000 title claims abstract description 17
- 239000011552 falling film Substances 0.000 claims abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 239000013078 crystal Substances 0.000 claims abstract description 32
- 239000012530 fluid Substances 0.000 claims abstract description 21
- 239000012452 mother liquor Substances 0.000 claims abstract description 20
- 238000004821 distillation Methods 0.000 claims abstract description 13
- 239000002562 thickening agent Substances 0.000 claims abstract description 13
- 239000012153 distilled water Substances 0.000 claims abstract description 9
- 238000007599 discharging Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims description 44
- 239000007788 liquid Substances 0.000 claims description 38
- 238000001704 evaporation Methods 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 23
- 239000012141 concentrate Substances 0.000 claims description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 18
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 claims description 14
- 239000002351 wastewater Substances 0.000 claims description 13
- 238000005119 centrifugation Methods 0.000 claims description 10
- 230000008020 evaporation Effects 0.000 claims description 10
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 8
- 239000013043 chemical agent Substances 0.000 claims description 8
- 229910052804 chromium Inorganic materials 0.000 claims description 8
- 239000011651 chromium Substances 0.000 claims description 8
- 238000005342 ion exchange Methods 0.000 claims description 7
- 150000003839 salts Chemical class 0.000 claims description 7
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 5
- 230000001376 precipitating effect Effects 0.000 claims description 5
- 238000004062 sedimentation Methods 0.000 claims description 4
- 238000010025 steaming Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 4
- -1 centrifuge Substances 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 239000010865 sewage Substances 0.000 abstract description 2
- 238000001223 reverse osmosis Methods 0.000 description 6
- 150000002500 ions Chemical class 0.000 description 5
- 239000012528 membrane Substances 0.000 description 5
- 238000002425 crystallisation Methods 0.000 description 4
- 230000008025 crystallization Effects 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 229910001385 heavy metal Inorganic materials 0.000 description 4
- 239000010408 film Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000001351 cycling effect Effects 0.000 description 2
- 239000006260 foam Substances 0.000 description 2
- 239000010808 liquid waste Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 238000002207 thermal evaporation Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/048—Purification of waste water by 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
- C02F1/06—Flash 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
- C02F2101/18—Cyanides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
- C02F2101/22—Chromium or chromium compounds, e.g. chromates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- 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
Landscapes
- 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 present invention relates to sewage-treatment plant technical field more particularly to a kind of electroplating waste processing process and device.Pass through sequentially connected original fluid container, feed pump, the first plate heat exchanger, the second plate heat exchanger, falling film evaporator, falling film separator, forced circulation heat exchanger, crystal separator, discharging pump, thickener, centrifuge, mother liquor tank；The falling film separator is connect by centrifugal compressor with falling film evaporator with crystal separator top；The falling film evaporator and forced circulation heat exchanger are also connected with distillation water pot, which is connect by distilled water pump with the first plate heat exchanger；The falling film separator, falling film evaporator, crystal separator are all connected with the input terminal of forced circulation pump, and the output end of the forced circulation pump is connect with forced circulation heat exchanger；A kind of electroplating waste processing process and device is set to save production cost, and high treating effect.
Description
Technical field
The present invention relates to sewage-treatment plant technical field more particularly to a kind of electroplating waste processing process and device.
Background technique
The water quality of electroplating wastewater is complicated, and ingredient is not easy to control, wherein containing the heavy metals such as chromium, cadmium, nickel, copper, zinc, gold, silver
The extremely toxic substances such as ion and cyanide also contain partial organic substances and a large amount of salt；The precipitation method invest waste water in electroplating wastewater at present
It is low, but effect is unstable, ion-exchange effect stability, simple process, can recycle the heavy metal in waste water, but put into
It is slightly higher, and salinity in water cannot be removed in the electroplating wastewater later period, salt content is higher in waste water.
Summary of the invention
The object of the present invention is to provide save production cost, and a kind of electroplating waste processing process and dress of high treating effect
It sets.
Technical scheme is as follows:
A kind of electroplating waste processing process, which comprises the following steps:
Step 1: stoste drops COD by activated carbon adsorber, removes Cr6+；
Step 2: flowing into sedimentation basin by the stoste of activated carbon adsorber, and chemical agent is added, remove cyanogen and chromium；
Step 3: the stoste after precipitating is filtered；
Step 4: ion exchange being carried out to filtered waste water, and by the material storing after ion exchange in original fluid container；
Step 5: the material in original fluid container being squeezed into the first, second plate heat exchanger by feed pump, is exchanged heat；
Step 6: the material after heat exchange is driven into falling film evaporator after reaching evaporating temperature, is evaporated concentration；
Step 7: the concentrate close to saturation after evaporation and concentration squeezed into forced circulation heat exchanger by transfering material pump carry out into
The concentration of one step；
Step 8: the material being further concentrated, which is driven into crystal separator, carries out flash concentration, concentrate and secondary steam
Vapor-liquid separation is carried out in crystal separator；Secondary steam after gas-liquid separation comes out from separator passes through centrifugal compressor liter
Falling film evaporator and forced circulation heat exchanger are squeezed into after temperature rise pressure；
Step 9: the concentrate in crystal separator bottom, which reaches, is pumped to thickener by discharging after discharge concentration；
Step 10: the material after stiff enters centrifuge centrifugation, and crystallizing and drying after centrifugation is packaged transmitting system, and from
Desuperheated mother liquor, which is squeezed into mother liquor tank, during the heart is heated；
Step 11: the concentrate after gas-liquid separation is forced circulating pump and squeezes into forced circulation heat exchanger, repeats step 7；
Step 12: the mother liquor heated in mother liquor fills is squeezed into forced circulation heat exchanger after reaching evaporating temperature by pump, weight
Multiple step 7.
COD drops, except Cr6+ etc. by activated carbon adsorber, chemical agent adds precipitating plus filtering removal cyanogen, chromium etc., and ion is handed over
Change the cyaniding complex anion of heavy-metal ion removal and some metals；Treating material (solution) is stored in original fluid container, warp
It crosses pretreated material to come out from original fluid container, the first, second plate heat exchanger is squeezed by feed pump, in the first plate heat exchanger
Interior feeding liquid and steam condensate (SC) carry out heat exchange, be warming up to after evaporating temperature and enter falling film evaporator, be evaporated concentration；
Material is by falling film evaporator, and in falling film evaporator tubulation, from top to down, by thermal evaporation, concentrate falls to down tube to material
Material reaches higher concentration after case；It is delivered in forced circulation heat exchanger by transfering material pump and continues evaporating, concentrating and crystallizing；Material exists
Into forced circulation heat exchanger increasing temperature and pressure, it is then admitted to crystal separator, and carries out flash concentration in crystal separator；
Concentrate and secondary steam carry out vapor-liquid separation in crystal separator, and the concentrate after gas-liquid separation is forced circulating pump and squeezes into
Forced circulation heat exchanger, concentrate continue to heat up in forced circulation heat exchanger, enter crystal separator afterwards, in separator
Interior carry out flash concentration so recycles；And concentrate will be pumped into thickener after reaching discharge concentration；Object in thickener
Expect that entering centrifuge after stiff is centrifuged, the crystallizing and drying after centrifugation is packaged, and desuperheated mother liquor is through adding in centrifugal process
Reach evaporating temperature return system after heat to continue to be concentrated by evaporation；The secondary steam come out from separator, into compressor system
System；After secondary steam is compressed, temperature can be increased to 101 DEG C or so, and compressed steam is squeezed into forced circulation heat exchanger again and added
Thermal material；It is increased to 101 DEG C of steam after material after preheated enters falling film evaporator, and after compression and carries out heat exchange evaporation,
Whole system reaches thermal balance.
During step 7 heated material, the steam of heating is condensed into water and flow in distillation water pot, and passes through distillation
Water pump is squeezed into the first plate heat exchanger.During heated material, this portion temperature is about that 101 DEG C of steam is condensed into water
It flow to condensate to fill and be pumped into plate heat exchanger and material liquid heat exchange by distilled water pump, temperature is down to 35 DEG C or so discharge systems.
Steam after exchanging heat in step 6 enters squeezes into centrifugal compressor again after gas-liquid separation in falling film separator
It is interior.Since falling film evaporator evaporation capacity is larger, steam will carry out gas-liquid separation by falling film separator before entering centrifugal compressor,
To extend the service life of compressor.
Chemical agent in step 2 uses broken cyanide agent.The removal cyanogen in waste water can be preferably removed using broken cyanide agent
And chromium.
A kind of electroplating wastewater processing vaporising device, which is characterized in that including sequentially connected original fluid container, feed pump,
One plate heat exchanger, the second plate heat exchanger, falling film evaporator, falling film separator, forced circulation heat exchanger, crystal separator,
Discharging pump, thickener, centrifuge, mother liquor tank；The falling film separator and crystal separator top pass through centrifugal compressor and drop
Film evaporator connection；The falling film evaporator and forced circulation heat exchanger are respectively connected with distillation water pot, which passes through steaming
Distilled water pump is connect with the first plate heat exchanger；The falling film separator, falling film evaporator, crystal separator are all connected with forced circulation
The output end of the input terminal of pump, the forced circulation pump is connect with forced circulation heat exchanger.By original fluid container store stoste, by into
Stoste is transmitted in the first, second plate heat exchanger by material pump to exchange heat；By the way that falling film evaporator is arranged, forcing waste liquid
Enter in crystal separator after temperature-pressure in circulating evaporator and crystallized, by thickener stiff and squeezes into centrifugation again after crystallization
Machine is packaged after being centrifuged by centrifuge and sends out, to realize the separation of salt water；And in centrifugal process, liquefied crystallization flows into
Heating in mother liquor tank is squeezed into crystal separator by pump after reaching evaporating temperature, is continued cycling through.
The original fluid container is also connected with reverse osmosis unit；The reverse osmosis unit includes high-pressure pump and water tank；The storage
The semi-permeable membrane that water tank is divided into upper cavity and lower chamber is equipped in water pot, which is connected to high-pressure pump, lower chamber and
Distill water pot connection；The upper cavity is also connect with original fluid container.The waste liquid in atmospheric distillation tower is squeezed into epicoele by high-pressure pump
In body, due to the design using semi-permeable membrane, the pressure of upper cavity is larger, and the moisture in waste liquid will flow into lower chamber, and on
The intracorporal liquid waste concentration of chamber will also increase；Since lower chamber is connected to distillation water pot, the intracorporal water of cavity of resorption, which will flow into, to be distilled
It is collected in water pot, and the concentrated solution containing salt will exchange heat in the first plate heat exchanger of inflow in upper cavity.
Second separator is also connected between the falling film separator, crystal separator and compressor.It is secondary by being arranged
Separator carries out gas-liquid separation again, allows steam entrained liquids foam as far as possible into compressor, protects compressor, does not prolong
Long compressor service life.
Detailed description of the invention
Through the following detailed description taken in conjunction with the accompanying drawings, present invention objects, features and advantages above-mentioned and other will become
Obviously.
Wherein: Fig. 1 is schematic structural view of the invention；
Fig. 2 is present system schematic illustration；
Fig. 3 is reverse osmosis unit structural schematic diagram of the present invention；
In attached drawing, 1 is original fluid container, and 2 be feed pump, and 3 be the first plate heat exchanger, and 4 be the second plate heat exchanger, and 5 be drop
Film evaporator, 6 be forced circulation heat exchanger, and 7 be crystal separator, and 8 be discharging pump, and 9 be thickener, and 10 be centrifuge, and 11 are
Mother liquor tank, 12 be centrifugal compressor, and 13 be distillation water pot, and 14 be distilled water pump, and 15 be forced circulation pump, and 16 be high-pressure pump, 17
It is semi-permeable membrane for water tank, 18,19 be activated carbon adsorber, and 20 be sedimentation basin, and 21 be second separator, and 22 separate for falling liquid film
Device.
Specific embodiment
A kind of electroplating waste processing process, which comprises the following steps:
Step 1: stoste drops COD by activated carbon adsorber, removes Cr6+；
Step 2: flowing into sedimentation basin by the stoste of activated carbon adsorber, and chemical agent is added, remove cyanogen and chromium；
Step 3: the stoste after precipitating is filtered；
Step 4: ion exchange being carried out to filtered waste water, and by the material storing after ion exchange in original fluid container；
Step 5: the material in original fluid container being squeezed into the first, second plate heat exchanger by feed pump, is exchanged heat；
Step 6: the material after heat exchange is driven into falling film evaporator after reaching evaporating temperature, is evaporated concentration；
Step 7: the concentrate after evaporation and concentration close to saturation is squeezed into forced circulation heat exchanger by transfering material pump to carry out into one
Step heating concentration；
Step 8: the material being further concentrated, which is driven into crystal separator, carries out flash concentration, concentrate and secondary steam
Vapor-liquid separation is carried out in crystal separator；Secondary steam after gas-liquid separation comes out from separator passes through centrifugal compressor liter
Falling film evaporator and forced circulation heat exchanger are squeezed into after temperature rise pressure；
Step 9: the concentrate in crystal separator bottom, which reaches, is pumped to thickener by discharging after discharge concentration；
Step 10: the material after stiff enters centrifuge centrifugation, and crystallizing and drying after centrifugation is packaged transmitting system, and from
Desuperheated mother liquor, which is squeezed into mother liquor tank, during the heart is heated；
Step 11: the concentrate after gas-liquid separation is forced circulating pump and squeezes into forced circulation heat exchanger, repeats step 7；
Step 12: the mother liquor heated in mother liquor fills is squeezed into forced circulation heat exchanger after reaching evaporating temperature by pump, weight
Multiple step 7.COD drops, except Cr6+ etc. by activated carbon adsorber, chemical agent adds precipitating plus filtering removal cyanogen, chromium etc., and ion is handed over
Change the cyaniding complex anion of heavy-metal ion removal and some metals；Treating material (solution) is stored in original fluid container, warp
It crosses pretreated material to come out from original fluid container, the first, second plate heat exchanger is squeezed by feed pump, in the first plate heat exchanger
Interior feeding liquid and steam condensate (SC) carry out heat exchange, be warming up to after evaporating temperature and enter falling film evaporator, be evaporated concentration；
Material is by falling film evaporator, and in falling film evaporator tubulation, from top to down, by thermal evaporation, concentrate falls to down tube to material
Material reaches higher concentration after case；It is delivered in forced circulation heat exchanger by transfering material pump and continues evaporating, concentrating and crystallizing；Material exists
Into forced circulation heat exchanger increasing temperature and pressure, it is then admitted to crystal separator, and carries out flash concentration in crystal separator；
Concentrate and secondary steam carry out vapor-liquid separation in crystal separator, and the concentrate after gas-liquid separation is forced circulating pump and squeezes into
Forced circulation heat exchanger, concentrate continue to heat up in forced circulation heat exchanger, enter crystal separator afterwards, in separator
Interior carry out flash concentration so recycles；And concentrate will be pumped into thickener after reaching discharge concentration；Object in thickener
Expect that entering centrifuge after stiff is centrifuged, the crystallizing and drying after centrifugation is packaged, and desuperheated mother liquor is through adding in centrifugal process
Reach evaporating temperature return system after heat to continue to be concentrated by evaporation；The secondary steam come out from separator, into compressor system
System；After secondary steam is compressed, temperature can be increased to 101 DEG C or so, and compressed steam is squeezed into forced circulation heat exchanger again and added
Thermal material；It is increased to 101 DEG C of steam after material after preheated enters falling film evaporator, and after compression and carries out heat exchange evaporation,
Whole system reaches thermal balance.
Preferably, during step 7 heated material, the steam of heating is condensed into water and flow in distillation water pot, and
It is squeezed into the first plate heat exchanger by distilled water pump.During heated material, this portion temperature is about 101 DEG C of steam
It is condensed into water to flow to condensate filling and be pumped into plate heat exchanger and material liquid heat exchange by distilled water pump, temperature is down to 35 DEG C or so discharges
System.
Preferably, chemical agent in step 2 uses the agent of ITO broken cyanide.Waste water can preferably be removed using broken cyanide agent
In removal cyanogen and chromium.
Preferably, waste liquid after filtering can be squeezed into reverse osmosis unit in step 4, after carrying out a preliminary filtering,
It squeezes into original fluid container again.
Preferably, the steam after exchanging heat in step 6 enters squeezes into centrifugation again after gas-liquid separation in falling film separator
In compressor.Since falling film evaporator evaporation capacity is larger, steam will carry out gas by falling film separator before entering centrifugal compressor
Liquid separation, to extend the service life of compressor.
Preferably, the steam in crystal separator and falling film separator carries out gas-liquid point by second separator again
From.Entrained liquids do not enter compressor to the steam for making into centrifugal compressor as far as possible, extend the service life of compressor.
Shown in referring to figures 1-3, a kind of electroplating wastewater processing vaporising device, including sequentially connected original fluid container 1, charging
Pump the 2, first plate heat exchanger 3, the second plate heat exchanger 4, falling film evaporator 5, falling film separator, forced circulation heat exchanger 6, knot
Brilliant separator 7, discharging pump 8, thickener 9, centrifuge 10, mother liquor tank 11；The falling film separator 22 and crystal separator top
It is connect by centrifugal compressor 12 with falling film evaporator；The falling film evaporator and forced circulation heat exchanger are respectively connected with distilled water
Tank 13, the distillation water pot are connect by distilled water pump 14 with the first plate heat exchanger；The falling film separator, falling film evaporator,
Crystal separator is all connected with the input terminal of forced circulation pump 15, and the output end and forced circulation heat exchanger of the forced circulation pump connect
It connects.Stoste is stored by original fluid container, stoste is transmitted in the first, second plate heat exchanger by feed pump and is exchanged heat；It is logical
Setting falling film evaporator is crossed, enters waste liquid in crystal separator after temperature-pressure in forced-circulation evaporator and is crystallized,
By thickener stiff and centrifuge is squeezed into again after crystallization, is packaged and sends out after being centrifuged by centrifuge, to realize the separation of salt water；
And in centrifugal process, liquefied crystallization flows into heating in mother liquor tank, reaches and squeezes into crystal separator by pump after evaporating temperature
It is interior, it continues cycling through；Wherein by setting falling film separator, since falling film evaporator evaporation capacity is larger, before steam enters compressor
Gas-liquid separation is carried out by falling film separator, in case the liquid that entrainment with steam is excessive, damages compressor.
The original fluid container is also connected with reverse osmosis unit；The reverse osmosis unit includes high-pressure pump 16 and water tank 17；Institute
The semi-permeable membrane 18 for being equipped in water tank and water tank being divided into upper cavity and lower chamber is stated, which is connected to high-pressure pump, under
Cavity is connected to distillation water pot；The upper cavity is also connect with original fluid container.The waste liquid in atmospheric distillation tower is beaten by high-pressure pump
Enter in upper cavity, due to the design using semi-permeable membrane, the pressure of upper cavity is larger, and the moisture in waste liquid will flow into lower chamber
In, and the intracorporal liquid waste concentration of epicoele will also increase；Since lower chamber is connected to distillation water pot, the intracorporal water of cavity of resorption will flow
Enter to distill in water pot and collect, and the concentrated solution containing salt will exchange heat in the first plate heat exchanger of inflow in upper cavity.
Second separator 21 is also connected between the falling film separator, crystal separator and compressor.Pass through setting two
Secondary separator carries out gas-liquid separation again, allows steam not entrained liquids foam as far as possible into compressor, protects compressor,
Extend compressor service life.
Second heat exchanger plates, which change, to be also connected with vacuum pump plate and changes.It is changed by the way that vacuum pump plate is arranged, so that cooling fixed gas.
The above is only presently preferred embodiments of the present invention, not does limitation in any form to the present invention, it is all according to
According to any simple modification to the above embodiments in technical spirit of the invention, equivalent variations, guarantor of the invention is each fallen within
Within the scope of shield.
Claims (4)
1. a kind of electroplating waste processing process, which comprises the following steps:
Step 1: stoste drops COD by activated carbon adsorber, removes Cr6+；
Step 2: flowing into sedimentation basin by the stoste of activated carbon adsorber, and chemical agent is added, remove cyanogen and chromium；
Step 3: the stoste after precipitating is filtered；
Step 4: ion exchange being carried out to filtered waste water, and by the material storing after ion exchange in original fluid container；
Step 5: the material in original fluid container being squeezed into the first, second plate heat exchanger by feed pump, is exchanged heat；
Step 6: the material after heat exchange is driven into falling film evaporator after reaching evaporating temperature, is evaporated concentration；
Step 7: the concentrate close to saturation after evaporation and concentration is squeezed into forced circulation heat exchanger by transfering material pump to carry out further
Concentration；
Step 8: the material being further concentrated, which is driven into crystal separator, carries out flash concentration, and concentrate and secondary steam are being tied
Gas-liquid separation is carried out in brilliant separator；Secondary steam after gas-liquid separation comes out from separator to be heated up by centrifugal compressor
Falling film evaporator and forced circulation heat exchanger are squeezed into after boosting；
Step 9: the concentrate in crystal separator bottom, which reaches, is pumped to thickener by discharging after discharge concentration；
Step 10: the material after stiff enters centrifuge centrifugation, and the salt crystallizing and drying after centrifugation is packaged transmitting system, and is being centrifuged
Desuperheated mother liquor, which is squeezed into mother liquor tank, in the process is heated；
Step 11: the concentrate after gas-liquid separation is forced circulating pump and squeezes into forced circulation heat exchanger, repeats step 7；
Step 12: the mother liquor heated in mother liquor fills is squeezed into forced circulation heat exchanger after reaching evaporating temperature by pump, repeats to walk
Rapid 7.
2. a kind of electroplating waste processing process according to claim 1, which is characterized in that in the mistake of step 7 heated material
Cheng Zhong, the steam of heating is condensed into water and flow in distillation water pot, and is squeezed into the first plate heat exchanger by distilled water pump.
3. a kind of electroplating waste processing process according to claim 1, which is characterized in that the steaming after exchanging heat in step 6
Vapour enters in falling film separator to be squeezed into centrifugal compressor again after gas-liquid separation.
4. a kind of electroplating waste processing process according to claim 1, which is characterized in that chemical agent in step 2
Using broken cyanide agent.
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