CN106698792A - Organic salt-containing wastewater treatment system based on vacuum evaporation and thermal energy utilization and process - Google Patents
Organic salt-containing wastewater treatment system based on vacuum evaporation and thermal energy utilization and process Download PDFInfo
- Publication number
- CN106698792A CN106698792A CN201710015501.0A CN201710015501A CN106698792A CN 106698792 A CN106698792 A CN 106698792A CN 201710015501 A CN201710015501 A CN 201710015501A CN 106698792 A CN106698792 A CN 106698792A
- Authority
- CN
- China
- Prior art keywords
- water
- steam
- waste water
- wastewater
- concentration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 44
- 150000003839 salts Chemical class 0.000 title claims abstract description 27
- 238000004065 wastewater treatment Methods 0.000 title abstract description 16
- 238000007738 vacuum evaporation Methods 0.000 title abstract description 8
- 238000001704 evaporation Methods 0.000 claims abstract description 150
- 239000002351 wastewater Substances 0.000 claims abstract description 146
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 75
- 230000003647 oxidation Effects 0.000 claims abstract description 61
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 61
- 238000007906 compression Methods 0.000 claims abstract description 51
- 230000008020 evaporation Effects 0.000 claims abstract description 42
- 238000002425 crystallisation Methods 0.000 claims abstract description 31
- 230000008025 crystallization Effects 0.000 claims abstract description 31
- 238000010438 heat treatment Methods 0.000 claims abstract description 19
- 230000006835 compression Effects 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 9
- 238000003860 storage Methods 0.000 claims abstract description 9
- 239000012452 mother liquor Substances 0.000 claims abstract description 6
- 239000002699 waste material Substances 0.000 claims description 52
- 239000012267 brine Substances 0.000 claims description 45
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 45
- 229920006395 saturated elastomer Polymers 0.000 claims description 18
- 238000012545 processing Methods 0.000 claims description 11
- 239000010413 mother solution Substances 0.000 claims description 10
- 238000004064 recycling Methods 0.000 claims description 10
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 6
- 238000004382 potting Methods 0.000 claims description 6
- 238000010025 steaming Methods 0.000 claims description 6
- 239000005416 organic matter Substances 0.000 claims description 5
- 230000000630 rising effect Effects 0.000 claims description 4
- 238000005516 engineering process Methods 0.000 description 8
- 239000010842 industrial wastewater Substances 0.000 description 5
- 230000001590 oxidative effect Effects 0.000 description 5
- 238000009834 vaporization Methods 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000002904 solvent Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010504 bond cleavage reaction Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000005286 illumination Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000012546 transfer Methods 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
-
- 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
- C02F1/046—Treatment of water, waste water, or sewage by heating by distillation or evaporation under vacuum produced by a barometric column
-
- 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
- C02F2101/30—Organic compounds
-
- 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
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- 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)
Abstract
The invention discloses an organic salt-containing wastewater treatment system based on vacuum evaporation and thermal energy utilization and a process. The organic salt-containing wastewater treatment system comprises a wastewater storage tank, a heat exchanger, an oxidation device, a vacuum evaporation tank, a vacuum pump, a mechanical vapor compression pump and the like, wherein high-concentration organic salt-containing wastewater is firstly fed through the oxidation device; organic matters are oxidized and are degraded to release heat; then the temperature of the wastewater can be increased; after being further preheated by using a preheater, the wastewater is fed into the vacuum evaporation tank and is further heated by vapor generated after compression of the mechanical vapor compression pump; the pressure inside the vacuum evaporation tank is reduced; the wastewater can be rapidly evaporated to generate vapor; the vapor is fed into the mechanical vapor compression pump to improve the quality, and is used for heating the wastewater inside the vacuum evaporation tank to achieve evaporation; the vapor self is condensed into water which is fed into the preheater to preheat the oxidized wastewater. The evaporated concentrated wastewater is discharged out from the bottom of the vacuum evaporation tank, is circulated and evaporated by using a compulsive circulation pump, and is fed into a crystallization device to generate salt solids after certain concentration is met, and the mother liquor can be further circulated and evaporated.
Description
Technical field
The present invention relates to energy and environment field, more particularly to a kind of take into account the organic of heat energy utilization and contain based on being evaporated in vacuo
Salt Waste Water Treatment and technique.
Background technology
The treatment of high salt high concentrated organic wastewater has turned into problem in the industry, and exploring effective treatment technology has turned into useless
The study hotspot of water treatment field.In process of manufacture, portion of energy has finally been transferred to sewage in the way of heat transfer
In the middle of, meanwhile, the high-enriched organics in organic wastewater are in itself a kind of energy, if do not carried out sufficiently to this portion of energy
Reclaim and utilize, the waste of the energy will certainly be caused, and environment can be affected.Current Industrial Wastewater Treatment
Technology mainly reduces Pollutants in Wastewater concentration using the method for physics, chemistry and biology, reaches the standard that can be discharged, and
The heat energy contained in industrial wastewater is not paid close attention to.The inorganic salts of high-salt wastewater middle and high concentration are the suppression and murder by poisoning agent of microorganism,
The not up to standard of water quality can be caused.If heat energy utilization can be taken into account while water treatment effect is ensured, be on the one hand conducive to enterprise
The target of energy-saving and emission-reduction is realized, on the other hand new think of will be provided for the development of high salt Technology of High Concentration OrganicWastewater Treatment
Road.
The oxidation technology of organic wastewater is, using oxidant, electricity, illumination, catalyst etc., to open persistent organic pollutants
Ring, scission of link, substitution etc., macromolecular hardly degraded organic substance change into degradable small-molecule substance, or even directly generate CO2With
H2O.While organic wastewater oxidative degradation, amount of heat can be produced.So-called evaporation is will to contain the dilute of fixedness solute
Solution ebuillition of heated is concentrated, and makes volatile solvent part vaporization therein so as to solution be concentrated, to obtain solid product
Or solvent, actually fixedness solute and the separation process of volatile solvent are produced, by rationally control evaporating temperature, press
The parameters such as power, realize the purification of waste water.In Vacuum Evaporation Process, due to pressure reduction, it is converted into the part sensible heat in waste water
Gasification latent heat, produces steam, the heat of this some vapor rationally to utilize.
For organic brine waste, using oxidizing process by oxidation operation therein, degraded, and heat is released.High temperature gives up
Water evaporates into vacuum evaporator, is used after vapor condensation heat-exchange.In whole technical process, waste water is made full use of to carry
Heat, oxidation operation produce heat and evaporation after steam the latent heat of vaporization, while evaporation treatment waste water not receive waste water
The limitation of middle salinity, while water treatment effect is ensured, makes full use of the heat of waste water, is technology for treating industrial waste water
Development provides new thinking.
The content of the invention
In order to solve technical problem present in prior art, the present invention proposes that one kind takes into account heat energy utilization to be evaporated in vacuo
Organic brine waste processing system and method, propose different technical schemes for different operating mode.It is not very for concentration
Organic brine waste high, first with oxidizing process by the oxidation operation in waste water, degraded, and releases heat, after oxidation
By after preheating, into vacuum vaporation system, the steam after evaporation enters mechanical vapor-compression system to hot waste water, and steam is risen
Enter vacuum vaporation system after temperature rise pressure for waste water evaporation provides heat, steam is condensed into water, after heat can be used for pre- thermal oxide
Waste water, condensed water can do heat supply, process water or other.The recyclable evaporation of concentration waste water, reaches certain density saliferous and gives up
Water is by after crystallization, discharging salt solid.The organic brine waste higher for concentration, the hot waste water after oxidation directly enters
Enter vacuum vaporation system, omit preheating device, the condensed condensate temperature of steam is higher, can be used for heat supply, process water or
Other.In whole technical process, steam after the heat and evaporation that heat, oxidation operation that waste water carries are produced is made full use of
The latent heat of vaporization and sensible heat, while evaporation treatment waste water is not limited by salinity in waste water, are ensureing the same of water treatment effect
When, the heat of waste water is made full use of, for the development of technology for treating industrial waste water provides new thinking.
To achieve the above object, the present invention uses following technical proposals：
A kind of organic brine waste processing system that heat energy utilization is taken into account to be evaporated in vacuo, including wastewater storage tank, oxidation dress
Put, vacuum evaporating pot, vavuum pump, mechanical vapor-compression pump, forced circulation pump and crystallization apparatus；The wastewater storage tank outlet and oxygen
Makeup puts connected, and oxidation unit outlet is connected with heat exchanger waste line in vacuum evaporating pot, and vacuum evaporating pot top is provided with steaming
Vapor outlet is provided with concentration wastewater outlet and condensation-water drain with outlet, lower section is vacuumized；Described steam (vapor) outlet and mechanical vapour
Compression pump intake UNICOM, saturated vapor and the heat exchanger steam pipework in vacuum evaporating pot of mechanical vapor-compression pump discharge join
It is logical；It is described vacuumize outlet be connected with vavuum pump, vavuum pump intermittent duty；Concentration wastewater outlet and the circularly-supercharged pump intake
And crystallization apparatus are respectively connected with, the recyclable evaporation of concentration waste water enters crystallization apparatus after reaching finite concentration.
The technique processed organic brine waste using above-mentioned system：
The organic brine waste of high concentration first passes around oxidation unit, and organic matter is degraded heat release, wastewater temperature after peroxidating
Raise, into vacuum evaporating pot, further by the steam heating after mechanical vapor-compression pump pressure contracting, meanwhile, vacuum evaporating pot
Interior pressure reduction, waste water evaporates rapidly generation steam, and steam is used for heating, vacuum after entering mechanical vapor-compression pump lifting quality
, to realize evaporation, steam is condensed into water in itself for waste water in evaporator, condensed water can do process water or other；
Concentration waste water after evaporation, by forced circulation pump circulating and evaporating, reaches certain from pot bottom discharge is evaporated in vacuo
Enter crystallization apparatus after concentration and produce salt solid, the further circulating and evaporating of mother liquor.
The technique of described organic brine waste treatment, comprises the following steps that：
(1) the organic brine waste of high concentration enters oxidation unit, and oxidation operation degraded heat release, wastewater temperature is increased to
80-95 DEG C, into vacuum evaporating pot, further by the steam heating after mechanical vapor-compression pump pressure contracting；
(2) absolute pressure is 39-85kPa in vacuum evaporating pot, and evaporating temperature is 75-95 DEG C；After vacuum evaporating pot evaporation
Steam by mechanical vapor-compression pump pressure contracting after, vapor (steam) temperature pressure rises to 83-125 DEG C, 53- from 75-95 DEG C, 39-85kPa
232kPa；
(3) water is condensed into after 83-125 DEG C, the saturated vapor of 53-232kPa and 80-95 DEG C of wastewater heat exchange, waste water is heated
Evaporation；
(5) the condensed water temperature of saturated vapor is about 83-125 DEG C, steam condensate (SC) can be used as process water or other；
(7) the concentration waste water after evaporating loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is concentrated into
Salt is crystallized out into crystallization apparatus after finite concentration, Recycling Mother Solution returns vacuum evaporating pot.
Organic brine waste processing system of heat energy utilization is taken into account to be evaporated in vacuo, described in the foregoing system
Oxidation unit and vacuum evaporating pot between be additionally provided with a heat exchanger, oxidation unit outlet and preheater waterwater entrance UNICOM,
Preheater wastewater outlet is connected with heat exchanger waste line in vacuum evaporating pot；Condensation-water drain and preheater hot water inlet phase
Even.
Further, the heat exchanger may be alternatively provided in vacuum evaporating pot.
The technique processed organic brine waste using described system,
The organic brine waste of high concentration first passes around oxidation unit, and organic matter is degraded heat release, wastewater temperature after peroxidating
Raise；
After preheater is further preheated, into vacuum evaporating pot, after further being contracted by mechanical vapor-compression pump pressure
Steam heating；Meanwhile, pressure inside the tank reduction is evaporated in vacuo, waste water evaporates rapidly generation steam, and steam enters mechanical vapour pressure
For the waste water in heating vacuum vaporation tank to realize evaporation after contracting pump lifting quality, steam is condensed into water in itself, into preheating
Waste water after the pre- thermal oxide of device, condensed water can do process water or other；
Concentration waste water after evaporation, by forced circulation pump circulating and evaporating, reaches certain from pot bottom discharge is evaporated in vacuo
Enter crystallization apparatus after concentration and produce salt solid, the further circulating and evaporating of mother liquor.
The technique of described organic brine waste treatment,
(1) the organic brine waste of high concentration enters oxidation unit, and oxidation operation degraded heat release, wastewater temperature is increased to
40-95℃；40-95 DEG C of waste water is continuously heating to 80-95 DEG C into preheater；It is further mechanical into vacuum evaporating pot
Steam heating after both vapor compression pump pressure contracting；
(2) absolute pressure is 39-85kPa in vacuum evaporating pot, and evaporating temperature is 75-95 DEG C；
(3) steam after evaporating is by after mechanical vapor-compression pump pressure contracting, vapor (steam) temperature pressure is from 75-95 DEG C, 39-
85kPa rises to 83-125 DEG C, 53-232kPa；
(4) water is condensed into after 83-125 DEG C, the saturated vapor of 53-232kPa and 80-95 DEG C of wastewater heat exchange, waste water is heated
Evaporation；
(5) the condensed water temperature of saturated vapor is about 83-125 DEG C, and the waste water after oxidation is preheated by preheater,
40-95 DEG C of waste water is heated to 80-95 DEG C, and condensed water water temperature is down to 45-90 DEG C；
(6) steam condensate (SC) is arranged as required to heat exchanger and further reclaims heat；
(7) the concentration waste water after evaporating loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is concentrated into
Salt is crystallized out into crystallization apparatus after finite concentration, Recycling Mother Solution returns vacuum evaporating pot.
Further, waste water enters the follow-up temperature of continuing rising of vacuum evaporating pot in step (2), and wastewater temperature is poor with evaporating temperature to be set
It is set to 5-28 DEG C；
Further, steam temperature rise after mechanical vapor-compression pump pressure contracts is 8-30 DEG C, steam after compression in step (3)
It it is 3-30 DEG C with the waste water temperature difference.
Further, the mode of oxidizing of the oxidation unit determines according to the property of waste water organic principle.
Beneficial effects of the present invention are as follows：
(1) in whole technical process, the heat that the heat of waste water carrying, oxidation operation are produced is fully utilized, and makes to give up
Water heats up for flashing；
(2) steam further compresses into Mechanical Vapor Compression after evaporating, and improving temperature and pressure is used to preheat raw water,
The latent heat of vaporization of steam is utilized；
(3) the condensed water water quality after evaporation treatment waste water is good, while water treatment effect is ensured, makes full use of useless
The heat of water, for the development of technology for treating industrial waste water provides new thinking.
Brief description of the drawings
The Figure of description for constituting the part of the application is used for providing further understanding of the present application, and the application's shows
Meaning property embodiment and its illustrated for explaining the application, does not constitute the improper restriction to the application.
Fig. 1 is based on being evaporated in vacuo the organic brine waste processing system figure of high concentration for taking into account heat energy utilization；
Fig. 2 is based on being evaporated in vacuo the organic brine waste processing system figure of high concentration for taking into account heat energy utilization；
In figure：1- waste water tanks/pond, 2- oxidation units, 3- preheaters, 4- vacuum evaporating pots, 5- mechanical vapor-compression pumps, 6-
Crystallization apparatus, 7- forced circulation pumps, 8- vavuum pumps
Specific embodiment
The present invention is further described with reference to the accompanying drawings and examples.
It is noted that described further below is all exemplary, it is intended to provide further instruction to the application.Unless another
Indicate, all technologies used herein and scientific terminology are with usual with the application person of an ordinary skill in the technical field
The identical meanings of understanding.
It should be noted that term used herein above is merely to describe specific embodiment, and be not intended to restricted root
According to the illustrative embodiments of the application.As used herein, unless the context clearly indicates otherwise, otherwise singulative
Be also intended to include plural form, additionally, it should be understood that, when in this manual use term "comprising" and/or " bag
Include " when, it indicates existing characteristics, step, operation, device, component and/or combinations thereof.
Embodiment 1：
As shown in figure 1, be not organic brine waste very high for concentration, its organic brine waste processing system, including
Wastewater storage tank, oxidation unit, preheater, vacuum evaporating pot, vavuum pump, mechanical vapor-compression pump, forced circulation pump and crystallization dress
Put；The wastewater storage tank outlet is connected with oxidation unit, and oxidation unit is exported and preheater waterwater entrance UNICOM, preheater waste water
Outlet is connected with heat exchanger waste line in vacuum evaporating pot, and vacuum evaporating pot top is provided with steam (vapor) outlet and vacuumizes outlet,
Lower section is provided with concentration wastewater outlet and condensation-water drain；The steam (vapor) outlet and mechanical vapor-compression pump intake UNICOM, machinery steam
Heat exchanger steam pipework UNICOM in the saturated vapor and vacuum evaporating pot of vapour pressure contracting pump discharge；The condensation-water drain and preheating
Device hot water inlet is connected；The concentration wastewater outlet is respectively connected with circularly-supercharged pump intake and crystallization apparatus, and concentration waste water can
Circulating and evaporating, reaches and enters crystallization apparatus after finite concentration, described to vacuumize outlet and be connected with vavuum pump, vavuum pump intermittently fortune
OK.
The organic brine waste of high concentration first passes around oxidation unit, and organic matter is degraded heat release, wastewater temperature after peroxidating
Raise, after preheater is further preheated, into vacuum evaporating pot, further by the steaming after mechanical vapor-compression pump pressure contracting
Vapour is heated, meanwhile, pressure inside the tank reduction is evaporated in vacuo, waste water evaporates rapidly generation steam, and steam enters mechanical vapor-compression pump
For the waste water in heating vacuum vaporation tank to realize evaporation after lifting quality, steam is condensed into water in itself, pre- into preheater
Waste water after thermal oxide, condensed water can do process water or other.Concentration waste water after evaporation is discharged from pot bottom is evaporated in vacuo,
By forced circulation pump circulating and evaporating, crystallization apparatus generation salt solid is entered after reaching finite concentration, mother liquor is further circulated
Evaporation.
In above-mentioned Waste Water Treatment, the organic brine waste of high concentration first passes around oxidation unit so that organic
Thing degraded heat release, wastewater temperature is raised.
In above-mentioned Waste Water Treatment, the oxidation unit is connected with preheater, and waste water is further in preheater
Heating, thermal source used is follow-up steam condensate (SC).
In above-mentioned Waste Water Treatment, the waste water after preheating enters vacuum evaporating pot and absorbs the heat from steam after compression
Amount evaporation.
In above-mentioned Waste Water Treatment, after the steam after evaporation enters mechanical vapor-compression pump increasing temperature and pressure, return true
The empty pre- thermal wastewater of evaporator, steam is condensed into water, can be arranged as required to heat exchanger and further reclaim heat, and condensed water can do
Process water or other.
In above-mentioned Waste Water Treatment, concentration waste water reaches finite concentration laggard by forced circulation pump circulating and evaporating
Enter crystallization apparatus, discharge salt solid, Recycling Mother Solution returns vacuum evaporating pot evaporation.
In above-mentioned Waste Water Treatment, the vacuum in vacuum evaporating pot is provided by vavuum pump, vavuum pump intermittent duty.
For said system, based on being evaporated in vacuo, the high concentration of taking into account heat energy utilization is organic to be contained present invention also offers a kind of
Salt waste water treatment process, comprises the following steps：
(1) the organic brine waste of high concentration enters oxidation unit, and oxidation operation degraded heat release, wastewater temperature is increased to
40-95℃；
(2) 40-95 DEG C of waste water is continuously heating to 80-95 DEG C into preheater, and thermal source is for after mechanical vapor-compression pump
The condensed condensed water of compressed steam, absolute pressure is 39-85kPa in vacuum evaporating pot, and evaporating temperature is 75-95 DEG C；
(3) steam after evaporating is by after mechanical vapor-compression pump pressure contracting, vapor (steam) temperature pressure is from 75-95 DEG C, 39-
85kPa rises to 83-125 DEG C, 53-232kPa；
(4) water is condensed into after 83-125 DEG C, the saturated vapor of 53-232kPa and 80-95 DEG C of wastewater heat exchange, waste water is heated
Evaporation；
(5) the condensed water temperature of saturated vapor is about 83-125 DEG C, and the waste water after oxidation is preheated by preheater,
40-95 DEG C of waste water is heated to 80-95 DEG C, and condensed water water temperature is down to 45-90 DEG C；
(6) steam condensate (SC) can be used as process water or other, also dependent on need set heat exchanger further reclaim heat
Amount；
(7) the concentration waste water after evaporating loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is concentrated into
Salt is crystallized out into crystallization apparatus after finite concentration, Recycling Mother Solution returns vacuum evaporating pot.
Preferably, the wastewater temperature in step (1) after oxidation is 40-95 DEG C.
Preferably, waste water enters the follow-up temperature of continuing rising of vacuum evaporating pot in step (2), and wastewater temperature is poor with evaporating temperature to be set
It is set to 5-28 DEG C.
Preferably, steam temperature rise after mechanical vapor-compression pump pressure contracts is 8-30 DEG C, steam after compression in step (3)
It it is 3-30 DEG C with the waste water temperature difference.
The mode of oxidizing of the oxidation unit determines according to the property of waste water organic principle.
Before the vacuum evaporating pot heat exchanger may be provided in vacuum evaporating pot, may be alternatively provided in vacuum evaporating pot.
After the steam is condensed into water, heat exchanger can be set and realize further reclaiming heat in system, also can directly use
In heat supply or other, condensed water can be used for process water or other.
It is described concentration waste water by the way that forced circulation pump circulation is concentrated into finite concentration after enter crystallization apparatus, concentrate concentration by
The property of different salt is determined.
By above-mentioned technique, can be realized on the premise of heat energy utilization is taken into account at the purification of the organic brine waste of high concentration
Reason.
Specific embodiment is as follows：
COD contents enter oxidation unit for the organic brine waste of high concentration that 6000mg/L, NaCl content are about 8%, have
Machine thing complete oxidation degraded heat release, wastewater temperature is about increased to 40 DEG C from room temperature, and the waste water after oxidation is compressed into heat exchanger
Steam condensate (SC) is preheated to 95 DEG C, and absolute pressure is 58kPa in vacuum evaporating pot, and evaporating temperature is 85 DEG C, and waste water enters vacuum
Evaporator is by the compressed steam heating evaporation after mechanical vapor-compression pump；85 DEG C, the steam process machinery steaming of 58kPa after evaporation
The contracting of vapour pressure contracting pump pressure, 101 DEG C are turned into after spray cooling, 101 DEG C is condensed into after the saturated vapor of 105kPa, with wastewater heat exchange
Water, the waste water that steam condensate (SC) can be used for after pre- thermal oxide, own temperature is down to 45 DEG C or so, can be used for process water or its
He.Concentration waste water after evaporation loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is concentrated into finite concentration
Salt is crystallized out into crystallization apparatus afterwards, Recycling Mother Solution returns vacuum evaporating pot.
Embodiment 2：
As shown in Fig. 2 for concentration organic brine waste higher, its organic brine waste processing system, including it is useless
Water storage tank, oxidation unit, vacuum evaporating pot, vavuum pump, mechanical vapor-compression pump, forced circulation pump and crystallization apparatus；It is described useless
Water storage tank outlet is connected with oxidation unit, and oxidation unit outlet is connected with heat exchanger waste line in vacuum evaporating pot, and vacuum is steamed
Hair tank top is provided with steam (vapor) outlet and vacuumizes outlet, and lower section is provided with concentration wastewater outlet and condensation-water drain；Described steam
Outlet and mechanical vapor-compression pump intake UNICOM, the heat exchange in the saturated vapor and vacuum evaporating pot of mechanical vapor-compression pump discharge
Device steam pipework UNICOM；It is described vacuumize outlet be connected with vavuum pump, vavuum pump intermittent duty；It is described to concentrate wastewater outlet and follow
Ring is pressurized pump intake and crystallization apparatus are respectively connected with, the recyclable evaporation of concentration waste water, and crystallization apparatus are entered after reaching finite concentration.
In above-mentioned Waste Water Treatment, the organic brine waste of high concentration first passes around oxidation unit so that organic
Thing degraded heat release, wastewater temperature is raised.
In above-mentioned Waste Water Treatment, enter vacuum evaporating pot from oxidation unit waste water out and absorb from after compression
The heat of vaporization of steam.
In above-mentioned Waste Water Treatment, after the steam after evaporation enters mechanical vapor-compression pump increasing temperature and pressure, return true
The empty pre- thermal wastewater of evaporator, steam is condensed into water, condensed water can do process water or other.
In above-mentioned Waste Water Treatment, concentration waste water reaches finite concentration laggard by forced circulation pump circulating and evaporating
Enter crystallization apparatus, discharge salt solid, Recycling Mother Solution returns vacuum evaporating pot evaporation.
For dense organic brine waste, its organic brine waste handling process comprises the following steps：
(1) the organic brine waste of high concentration enters oxidation unit, and oxidation operation degraded heat release, wastewater temperature is increased to
80-95 DEG C, into vacuum evaporating pot, further by the steam heating after mechanical vapor-compression pump pressure contracting；
(2) absolute pressure is 39-85kPa in vacuum evaporating pot, and evaporating temperature is 75-95 DEG C；After vacuum evaporating pot evaporation
Steam by mechanical vapor-compression pump pressure contracting after, vapor (steam) temperature pressure rises to 83-125 DEG C, 53- from 75-95 DEG C, 39-85kPa
232kPa；
(3) water is condensed into after 83-125 DEG C, the saturated vapor of 53-232kPa and 80-95 DEG C of wastewater heat exchange, waste water is heated
Evaporation；
(5) the condensed water temperature of saturated vapor is about 83-125 DEG C, steam condensate (SC) can be used as process water or other；
(7) the concentration waste water after evaporating loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is concentrated into
Salt is crystallized out into crystallization apparatus after finite concentration, Recycling Mother Solution returns vacuum evaporating pot.
Specific embodiment is as follows：
COD contents enter oxidation unit for the organic brine waste of high concentration that 25000mg/L, NaCl content are about 8%, have
Machine thing complete oxidation degraded heat release, wastewater temperature is about increased to 95 DEG C from room temperature, and absolute pressure is 58kPa in vacuum evaporating pot,
Evaporating temperature is 85 DEG C, and waste water enters vacuum evaporating pot by the compressed steam heating evaporation after mechanical vapor-compression pump；After evaporation
85 DEG C, the steam of 58kPa by turning into 101 DEG C after the contracting of mechanical vapor-compression pump pressure, spray cooling, the saturation of 105kPa steams
101 DEG C of water is condensed into after vapour, with wastewater heat exchange, steam condensate (SC) can be used for heat supply, process water be done or other, after evaporation
Concentration waste water loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is filled into crystallization after being concentrated into finite concentration
Put and crystallize out salt, Recycling Mother Solution returns vacuum evaporating pot.
The place different from embodiment 1 is that waste water COD concentration is higher, and wastewater temperature rising is more after oxidation heat liberation, very
Without further preheating before empty evaporator, saturated vapor condensed water heat can seek further Land use systems.
Although above-mentioned be described with reference to accompanying drawing to specific embodiment of the invention, not to present invention protection model
The limitation enclosed, one of ordinary skill in the art should be understood that on the basis of technical scheme those skilled in the art are not
Need the various modifications made by paying creative work or deformation still within protection scope of the present invention.
Claims (10)
1. it is a kind of to take into account organic brine waste processing system of heat energy utilization being evaporated in vacuo, it is characterised in that including waste water storage
Tank, oxidation unit, vacuum evaporating pot, vavuum pump, mechanical vapor-compression pump, forced circulation pump and crystallization apparatus；The waste water storage
Tank outlet is connected with oxidation unit, and oxidation unit outlet is connected with heat exchanger waste line in vacuum evaporating pot, vacuum evaporating pot
Top is provided with steam (vapor) outlet and vacuumizes outlet, and lower section is provided with concentration wastewater outlet and condensation-water drain；Described steam (vapor) outlet
With mechanical vapor-compression pump intake UNICOM, saturated vapor and the heat exchanger in vacuum evaporating pot of mechanical vapor-compression pump discharge steam
Vapor pipeline UNICOM；It is described vacuumize outlet be connected with vavuum pump, vavuum pump intermittent duty；The concentration wastewater outlet increases with circulation
Press pump entrance and crystallization apparatus are respectively connected with, the recyclable evaporation of concentration waste water, and crystallization apparatus are entered after reaching finite concentration.
2. organic brine waste processing system of heat energy utilization is taken into account to be evaporated in vacuo as claimed in claim 1, and its feature exists
In, a heat exchanger is additionally provided between described oxidation unit and vacuum evaporating pot, oxidation unit is exported and preheater waste water
Entrance UNICOM, preheater wastewater outlet is connected with heat exchanger waste line in vacuum evaporating pot；Condensation-water drain and preheater hot
Water inlet is connected.
3. organic brine waste processing system of heat energy utilization is taken into account to be evaporated in vacuo as claimed in claim 2, and its feature exists
In the heat exchanger may be alternatively provided in vacuum evaporating pot.
4. the technique for being processed organic brine waste using the system described in claim 1, it is characterised in that
The organic brine waste of high concentration first passes around oxidation unit, and organic matter is degraded heat release after peroxidating, and wastewater temperature is raised；
Further by the steam heating after mechanical vapor-compression pump pressure contracting in into vacuum evaporating pot, meanwhile, in vacuum evaporating pot
Pressure reduction, waste water evaporates rapidly generation steam, and steam steams after entering mechanical vapor-compression pump lifting quality for heating, vacuum
To realize evaporation, steam is condensed into water to waste water in hair tank in itself, condensed water can do process water or other；
Concentration waste water after evaporation, by forced circulation pump circulating and evaporating, reaches finite concentration from pot bottom discharge is evaporated in vacuo
Enter crystallization apparatus afterwards and produce salt solid, the further circulating and evaporating of mother liquor.
5. the technique that organic brine waste as claimed in claim 4 is processed, it is characterised in that comprise the following steps that
(1) the organic brine waste of high concentration enters oxidation unit, and oxidation operation degraded heat release, wastewater temperature is increased to 80-95
DEG C, into vacuum evaporating pot；
(2) thermal source of vacuum evaporating pot is the condensed condensed water of compressed steam after mechanical vapor-compression pump, vacuum evaporating pot
Interior absolute pressure is 39-85kPa, and evaporating temperature is 75-95 DEG C；Steam after vacuum evaporating pot evaporation is by mechanical vapor-compression
After pump pressure contracting, vapor (steam) temperature pressure rises to 83-125 DEG C, 53-232kPa from 75-95 DEG C, 39-85kPa；
(3) it is condensed into water after 83-125 DEG C, the saturated vapor of 53-232kPa and 80-95 DEG C of wastewater heat exchange, waste water is heated steaming
Hair；
(4) the condensed water temperature of saturated vapor is about 83-125 DEG C, steam condensate (SC) can be used as process water or other；
(5) the concentration waste water after evaporating loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is concentrated into certain
Salt is crystallized out into crystallization apparatus after concentration, Recycling Mother Solution returns vacuum evaporating pot.
6. the technique for being processed organic brine waste using the system described in claim 2, it is characterised in that
The organic brine waste of high concentration first passes around oxidation unit, and organic matter is degraded heat release after peroxidating, and wastewater temperature is raised；
After preheater is further preheated, into vacuum evaporating pot, further by the steaming after mechanical vapor-compression pump pressure contracting
Vapour is heated, meanwhile, pressure inside the tank reduction is evaporated in vacuo, waste water evaporates rapidly generation steam, and steam enters mechanical vapor-compression pump
For the waste water in heating vacuum vaporation tank to realize evaporation after lifting quality, steam is condensed into water in itself, pre- into preheater
Waste water after thermal oxide, condensed water can do process water or other；
Concentration waste water after evaporation, by forced circulation pump circulating and evaporating, reaches finite concentration from pot bottom discharge is evaporated in vacuo
Enter crystallization apparatus afterwards and produce salt solid, the further circulating and evaporating of mother liquor.
7. the technique that organic brine waste as claimed in claim 6 is processed, it is characterised in that
(1) the organic brine waste of high concentration enters oxidation unit, and oxidation operation degraded heat release, wastewater temperature is increased to 40-95
℃；40-95 DEG C of waste water is continuously heating to 80-95 DEG C into preheater；Into vacuum evaporating pot, further by mechanical vapour pressure
Steam heating after contracting pump pressure contracting；
(2) absolute pressure is 39-85kPa in vacuum evaporating pot, and evaporating temperature is 75-95 DEG C；
(3) steam after evaporating is by after mechanical vapor-compression pump pressure contracting, vapor (steam) temperature pressure is from 75-95 DEG C, 39-85kPa liters
To 83-125 DEG C, 53-232kPa；
(4) it is condensed into water after 83-125 DEG C, the saturated vapor of 53-232kPa and 80-95 DEG C of wastewater heat exchange, waste water is heated steaming
Hair；
(5) the condensed water temperature of saturated vapor is about 83-125 DEG C, the waste water after oxidation is preheated by preheater, 40-
95 DEG C of waste water is heated to 80-95 DEG C, and condensed water water temperature is down to 45-90 DEG C；
(6) steam condensate (SC) is arranged as required to heat exchanger and further reclaims heat；
(7) the concentration waste water after evaporating loops back vacuum evaporating pot by forced circulation pump to be continued to heat concentration, is concentrated into certain
Salt is crystallized out into crystallization apparatus after concentration, Recycling Mother Solution returns vacuum evaporating pot.
8. the technique that organic brine waste as claimed in claim 7 is processed, it is characterised in that
Waste water enters the follow-up temperature of continuing rising of vacuum evaporating pot in step (2), and wastewater temperature is set as 5-28 DEG C with evaporating temperature difference.
9. the technique that organic brine waste as claimed in claim 7 is processed, it is characterised in that
Steam is 8-30 DEG C by temperature rise after mechanical vapor-compression pump pressure contracting in step (3), and steam is with the waste water temperature difference after compression
3-30℃。
10. the technique that organic brine waste as claimed in claim 7 is processed, it is characterised in that the oxidation of the oxidation unit
Mode determines according to the property of waste water organic principle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710015501.0A CN106698792A (en) | 2017-01-10 | 2017-01-10 | Organic salt-containing wastewater treatment system based on vacuum evaporation and thermal energy utilization and process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710015501.0A CN106698792A (en) | 2017-01-10 | 2017-01-10 | Organic salt-containing wastewater treatment system based on vacuum evaporation and thermal energy utilization and process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106698792A true CN106698792A (en) | 2017-05-24 |
Family
ID=58907197
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710015501.0A Pending CN106698792A (en) | 2017-01-10 | 2017-01-10 | Organic salt-containing wastewater treatment system based on vacuum evaporation and thermal energy utilization and process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106698792A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108150998A (en) * | 2017-12-22 | 2018-06-12 | 芜湖德司节能科技有限公司 | A kind of boiler blowdown water heat energy utilization method |
| CN110436681A (en) * | 2019-08-23 | 2019-11-12 | 中国恩菲工程技术有限公司 | The system for handling waste water |
| CN110981055A (en) * | 2019-12-02 | 2020-04-10 | 无锡绿都环保科技有限公司 | Wastewater treatment method and wastewater treatment system |
| CN111003738A (en) * | 2019-12-02 | 2020-04-14 | 无锡绿都环保科技有限公司 | Evaporation operation method and evaporation system |
| CN111559769A (en) * | 2020-04-26 | 2020-08-21 | 北京中矿未来科技集团有限公司 | Evaporative crystallization system and method for industrial wastewater difficult to degrade |
| CN111821714A (en) * | 2020-07-27 | 2020-10-27 | 华峰集团上海工程有限公司 | Polyamide is with continuous concentrated system of refined salt |
| CN111995150A (en) * | 2020-08-19 | 2020-11-27 | 广东闻扬环境科技有限公司 | Saline wastewater circulating treatment system and treatment method |
| CN112408528A (en) * | 2020-10-29 | 2021-02-26 | 武汉凯迪水务有限公司 | Anti-fouling blocking and self-cleaning MVR evaporation concentration system |
| CN112624465A (en) * | 2020-11-22 | 2021-04-09 | 山东奥美环境股份有限公司 | Low-energy-consumption hydrochloric acid wastewater recycling device and method |
| CN115910411A (en) * | 2023-01-04 | 2023-04-04 | 中国原子能科学研究院 | Radioactive waste liquid treatment method and system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4141829A (en) * | 1976-09-09 | 1979-02-27 | Bayer Aktiengesellschaft | Process for wet oxidation of organic substances |
| CN202030559U (en) * | 2011-04-29 | 2011-11-09 | 四川寰球油气工程有限公司 | Evaporation concentration device for treating wastewater in oil-gas field |
| CN103880232A (en) * | 2013-03-25 | 2014-06-25 | 北京纬纶华业环保科技股份有限公司 | Treatment system and method for organic salt-containing wastewater |
| CN105036441A (en) * | 2015-07-22 | 2015-11-11 | 深圳市捷晶能源科技有限公司 | Concentration crystallization device for carnallite waste water |
| CN105152909A (en) * | 2015-06-30 | 2015-12-16 | 山东省食品发酵工业研究设计院 | Concentration and crystallization device for sodium gluconate production and process |
| CN206512053U (en) * | 2017-01-10 | 2017-09-22 | 山东大学 | Based on the organic brine waste processing system for being evaporated in vacuo simultaneous heat energy utilization |
-
2017
- 2017-01-10 CN CN201710015501.0A patent/CN106698792A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4141829A (en) * | 1976-09-09 | 1979-02-27 | Bayer Aktiengesellschaft | Process for wet oxidation of organic substances |
| CN202030559U (en) * | 2011-04-29 | 2011-11-09 | 四川寰球油气工程有限公司 | Evaporation concentration device for treating wastewater in oil-gas field |
| CN103880232A (en) * | 2013-03-25 | 2014-06-25 | 北京纬纶华业环保科技股份有限公司 | Treatment system and method for organic salt-containing wastewater |
| CN105152909A (en) * | 2015-06-30 | 2015-12-16 | 山东省食品发酵工业研究设计院 | Concentration and crystallization device for sodium gluconate production and process |
| CN105036441A (en) * | 2015-07-22 | 2015-11-11 | 深圳市捷晶能源科技有限公司 | Concentration crystallization device for carnallite waste water |
| CN206512053U (en) * | 2017-01-10 | 2017-09-22 | 山东大学 | Based on the organic brine waste processing system for being evaporated in vacuo simultaneous heat energy utilization |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108150998A (en) * | 2017-12-22 | 2018-06-12 | 芜湖德司节能科技有限公司 | A kind of boiler blowdown water heat energy utilization method |
| CN110436681B (en) * | 2019-08-23 | 2024-05-28 | 中国恩菲工程技术有限公司 | System for treating wastewater |
| CN110436681A (en) * | 2019-08-23 | 2019-11-12 | 中国恩菲工程技术有限公司 | The system for handling waste water |
| CN110981055A (en) * | 2019-12-02 | 2020-04-10 | 无锡绿都环保科技有限公司 | Wastewater treatment method and wastewater treatment system |
| CN111003738A (en) * | 2019-12-02 | 2020-04-14 | 无锡绿都环保科技有限公司 | Evaporation operation method and evaporation system |
| CN111559769A (en) * | 2020-04-26 | 2020-08-21 | 北京中矿未来科技集团有限公司 | Evaporative crystallization system and method for industrial wastewater difficult to degrade |
| CN111821714A (en) * | 2020-07-27 | 2020-10-27 | 华峰集团上海工程有限公司 | Polyamide is with continuous concentrated system of refined salt |
| CN111995150A (en) * | 2020-08-19 | 2020-11-27 | 广东闻扬环境科技有限公司 | Saline wastewater circulating treatment system and treatment method |
| CN111995150B (en) * | 2020-08-19 | 2021-04-16 | 广东闻扬环境科技有限公司 | Saline wastewater circulating treatment system and treatment method |
| CN112408528A (en) * | 2020-10-29 | 2021-02-26 | 武汉凯迪水务有限公司 | Anti-fouling blocking and self-cleaning MVR evaporation concentration system |
| CN112624465A (en) * | 2020-11-22 | 2021-04-09 | 山东奥美环境股份有限公司 | Low-energy-consumption hydrochloric acid wastewater recycling device and method |
| CN115910411A (en) * | 2023-01-04 | 2023-04-04 | 中国原子能科学研究院 | Radioactive waste liquid treatment method and system |
| CN115910411B (en) * | 2023-01-04 | 2024-05-10 | 中国原子能科学研究院 | Radioactive waste liquid treatment method and system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106698792A (en) | Organic salt-containing wastewater treatment system based on vacuum evaporation and thermal energy utilization and process | |
| CN104211130B (en) | A kind of low-temperature evaporation condensing crystallizing system and method utilizing used heat | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN106495384A (en) | The technique that a kind of utilization organic contamination high-salt wastewater prepares industrial purified salt | |
| CN206512053U (en) | Based on the organic brine waste processing system for being evaporated in vacuo simultaneous heat energy utilization | |
| CN105582684A (en) | Mechanical compression and evaporation device for acid solution evaporation and recovery and treatment method thereof | |
| CN105329959A (en) | Organic waste water integrated processing system and method | |
| CN104973642A (en) | Method of treating salt-containing waste water with low-temperature waste heat in flue gas | |
| CN106915792A (en) | Wind-solar complementary seawater desalination device | |
| CN113277665A (en) | Method and device for treating high-concentration high-salinity wastewater through electrolytic evaporation | |
| CN216584272U (en) | Primary evaporation negative pressure desalting device for desalting high-salinity wastewater | |
| CN204125195U (en) | A kind of low-temperature evaporation condensing crystal system utilizing used heat | |
| CN208054949U (en) | Rotary evaporator and low-temperature evaporation condensing crystallizing equipment | |
| CN104973641B (en) | A kind of method that flue gas low-temperature Waste Heat Reuse is combined with processing brine waste | |
| CN110054342A (en) | A method of product salt is obtained to high organic wastewater processing with high salt | |
| CN212292878U (en) | Evaporating system based on flowing air | |
| CN211310912U (en) | Landfill leachate membrane concentrate evaporation concentration system | |
| CN103833094A (en) | Method for treating high-salinity wastewater | |
| CN211871446U (en) | Acid and alkali slurry treatment system suitable for garbage leachate | |
| KR20090018403A (en) | Apparatus and method for purifying waste-water using a distillation under reduced pressure | |
| CN204737747U (en) | System for adopt solar energy combination heating to make waste water evaporation purification treatment | |
| CN208856938U (en) | A kind of desulfurization wastewater concentration structure | |
| CN211004648U (en) | System for evaporating mother liquor secondary evaporation concentration to landfill leachate | |
| JP4052652B2 (en) | Water treatment method and equipment | |
| CN207770450U (en) | A kind of castoff processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170524 |
|
| RJ01 | Rejection of invention patent application after publication |