CN113880166A - High-concentration landfill leachate treatment process and device - Google Patents
High-concentration landfill leachate treatment process and device Download PDFInfo
- Publication number
- CN113880166A CN113880166A CN202111057201.1A CN202111057201A CN113880166A CN 113880166 A CN113880166 A CN 113880166A CN 202111057201 A CN202111057201 A CN 202111057201A CN 113880166 A CN113880166 A CN 113880166A
- Authority
- CN
- China
- Prior art keywords
- outlet
- liquid
- inlet
- landfill leachate
- vapor
- 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
- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims description 35
- 239000007788 liquid Substances 0.000 claims abstract description 91
- 239000002918 waste heat Substances 0.000 claims abstract description 37
- 238000011084 recovery Methods 0.000 claims abstract description 34
- 238000000926 separation method Methods 0.000 claims abstract description 34
- 238000001704 evaporation Methods 0.000 claims abstract description 30
- 230000008020 evaporation Effects 0.000 claims abstract description 30
- 238000000746 purification Methods 0.000 claims abstract description 21
- 238000005191 phase separation Methods 0.000 claims abstract description 18
- 238000009835 boiling Methods 0.000 claims abstract description 16
- 239000012071 phase Substances 0.000 claims abstract description 6
- 239000012808 vapor phase Substances 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 106
- 239000012153 distilled water Substances 0.000 claims description 65
- 239000007789 gas Substances 0.000 claims description 38
- 239000007921 spray Substances 0.000 claims description 34
- 238000005406 washing Methods 0.000 claims description 21
- 239000003513 alkali Substances 0.000 claims description 20
- 239000002253 acid Substances 0.000 claims description 19
- 239000007791 liquid phase Substances 0.000 claims description 16
- 239000000498 cooling water Substances 0.000 claims description 13
- 238000005554 pickling Methods 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000008400 supply water Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 3
- 230000001877 deodorizing effect Effects 0.000 claims 1
- 239000013078 crystal Substances 0.000 description 10
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 7
- 239000003344 environmental pollutant Substances 0.000 description 7
- 231100000719 pollutant Toxicity 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000004332 deodorization Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- -1 sulfuric acid Chemical compound 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 239000012855 volatile organic compound Substances 0.000 description 1
Images
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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
- B01D53/44—Organic components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/58—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
-
- 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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- 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
Abstract
The invention relates to a high-concentration landfill leachate treatment device.A MVR evaporation and separation system comprises a circulating evaporation separator and a vapor compressor; the circulating evaporation separator comprises a shell-and-tube heat exchanger and a baffling type vapor-liquid separator; the high-concentration landfill leachate after being heated in the waste heat recovery system enters the pipe through a circulating liquid inlet of the shell-and-tube heat exchanger and exchanges heat with steam outside the pipe so as to enable the high-concentration landfill leachate to reach a boiling point; the baffling type vapor-liquid separator is provided with a plurality of stages of chambers, wherein the first stage of chamber is a vapor-liquid two-phase separation chamber, and the other chambers are vapor-phase vapor-liquid deep separation defoaming chambers; the outlet in the tube of the shell-and-tube heat exchanger is connected with the vapor-liquid two-phase separation chamber; a secondary steam outlet of the steam phase vapor-liquid deep separation defoaming chamber at the last stage is connected with a secondary steam purification system; the purified secondary steam in the secondary steam purification system is heated and pressurized by a steam compressor and then enters the outside of the tube of the shell-and-tube heat exchanger. The problem of evaporimeter be applied to easy scale deposit of landfill leachate trade is solved.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a high-concentration landfill leachate treatment process and device.
Background
The high-concentration landfill leachate mainly comes from membrane concentrated solution generated by a biochemical treatment and membrane treatment process, membrane concentrated solution generated by a DTRO emergency process and concentrated solution generated by other treatment processes, contains refractory organic matters, ammonia nitrogen and various inorganic salts, is brownish black, cannot be biochemically treated, and meanwhile, because the salt content is higher, no proper reverse osmosis membrane can be subjected to reduction treatment at present. The high-concentration landfill leachate containing a large amount of pollutants seriously threatens surface water, underground water, soil environment and the like, cannot be directly discharged into the environment, and is a difficult problem which needs to be solved when various technologies are applied to leachate treatment by reasonable treatment and disposal.
The MVR (Mechanical Vapor Recompression) evaporation technology is an evaporation technology for recycling latent heat of steam, avoids energy waste caused by condensing and discharging secondary steam, saves a condensing system, simplifies equipment flow, greatly simplifies operation, meets the technical requirements of energy conservation and emission reduction in China at present, and is considered as a wastewater treatment technology with great development potential. MVR evaporation is a technique that uses secondary steam as heating steam after its temperature and pressure are raised by mechanical compression. The mechanical vapor recompression principle is shown in figure 1, waste water enters a system, is mixed with returned mother liquor and circulating liquid and then enters an evaporator, heat absorption and evaporation are carried out, evaporated steam (secondary steam) is sucked by a compressor, is input into the evaporator after compression, temperature and pressure rise and then is subjected to heat release and condensation, condensed water is used as water for other processes or is directly discharged after reaching the standard, evaporated concentrated waste water is precipitated in the form of crystals by solute dissolved in the waste water when the concentration reaches the saturation solubility, and then the concentrated waste water is changed into a mixture (crystal slurry) of the crystals and the mother liquor. The crystal slurry is discharged from the evaporator, most of the crystal slurry is used as circulating liquid to continue the process, and the other small part of the crystal slurry is discharged into a separator. The crystal and the mother liquid in the crystal slurry are separated by the separator, the separated mother liquid returns to the system to continue to participate in circulation, and the separated crystal can be used as solid waste to be buried or reused. Therefore, the salt and liquid separation of the high-concentration salt-containing wastewater is realized. The whole process shows that the method can completely treat the waste water and can realize the aim of zero discharge of the landfill leachate.
The evaporator form that can be applied to the MVR technique is more, because high enriched landfill leachate has high COD, high ammonia nitrogen, the high characteristics that contain the salt, ordinary traditional evaporator easily appears scale deposit, blocks up, heat exchange efficiency and descends the scheduling problem to bring about drawbacks such as operating cycle weak point, cleaning cost height, equipment life weak point, consequently select a suitable evaporator form to be the problem that the MVR technique is applied to high enriched landfill leachate at first needs to be solved.
In addition, although the MVR evaporation technology has solved the problem of energy waste, there still exists a problem to be solved in the treatment effect of wastewater: because the landfill leachate has the characteristics of high ammonia nitrogen and high COD, ammonia nitrogen and volatile organic compounds enter steam together, when the steam is cooled to be condensed water, pollutants enter the condensed water together, so that the discharged water cannot directly reach the standard and is discharged, subsequent advanced treatment is required, a process route and operation cost are increased to a certain extent, and therefore, the pollutants are directly removed from the steam by technical means, and the key problem which needs to be solved by the MVR technology is solved.
Disclosure of Invention
The invention aims to solve the technical problem of providing a high-concentration landfill leachate treatment process and a device, so as to overcome the defects in the prior art.
The technical scheme for solving the technical problems is as follows: a high-concentration landfill leachate treatment device comprises:
the system comprises a waste heat recovery system, an MVR evaporation separation system and a secondary steam purification system; the MVR evaporation separation system comprises a circulation evaporation separator and a vapor compressor; the circulating evaporation separator comprises a shell-and-tube heat exchanger and a baffling type vapor-liquid separator; the high-concentration landfill leachate after being heated in the waste heat recovery system enters the pipe through a circulating liquid inlet of the shell-and-tube heat exchanger and exchanges heat with steam outside the pipe so as to enable the high-concentration landfill leachate to reach a boiling point; the baffling type vapor-liquid separator is provided with a plurality of stages of chambers, wherein the first stage of chamber is a vapor-liquid two-phase separation chamber, and the other chambers are vapor-phase vapor-liquid deep separation defoaming chambers; the outlet in the tube of the shell-and-tube heat exchanger is connected with the vapor-liquid two-phase separation chamber; a secondary steam outlet of the steam phase vapor-liquid deep separation defoaming chamber at the last stage is connected with a secondary steam purification system; the purified secondary steam in the secondary steam purification system is heated and pressurized by a steam compressor and then enters the outside of the tube of the shell-and-tube heat exchanger.
The invention has the beneficial effects that: the MVR evaporation separation system adopts two processes of in-pipe heating and chamber evaporation separation, ensures that the landfill leachate only conducts heat and raises temperature in a heating part, does not generate evaporation concentration, and avoids the generation of crystals; meanwhile, the high flow rate design of 1.0-4.0 m/s in the pipe is adopted, so that the inner wall of the pipe is flushed at a high speed at a high flow rate in the pipe, and the sedimentation and scaling of pollutants on the inner wall of the pipe are controlled, so that the problem that the evaporator is easy to scale when applied to the landfill leachate industry is effectively solved;
aiming at the problem that secondary steam generated in the traditional evaporation process contains ammonia nitrogen and organic matters, the secondary steam generated by the MVR evaporation separation system can be quickly subjected to vapor-liquid separation after being generated, and in addition, a multi-stage centrifugal separation principle is adopted in a separation section, so that salt mist and the like carried in the secondary steam are separated as far as possible.
On the basis of the technical scheme, the invention can be further improved as follows.
Further, the MVR evaporative separation system further includes:
and an inlet of the forced circulation pump is connected with a high-concentration garbage leachate outlet of the waste heat recovery system, and an outlet of the forced circulation pump is connected with a circulation liquid inlet of the shell-and-tube heat exchanger.
Further, a concentrated solution outlet of the vapor-liquid two-phase separation chamber is communicated with a circulating solution inlet of the forced circulation pump.
Further, the waste heat recovery system includes:
the inlet of the water inlet pump is externally connected with a high-concentration landfill leachate pipeline, and the outlet of the water inlet pump is provided with two branches;
the inlet of the concentrated liquid pump is connected with the concentrated liquid outlet of the vapor-liquid two-phase separation chamber, and the outlet of the concentrated liquid pump is connected with an outward conveying pipeline;
a cold side inlet of the distilled water heater is connected with one branch of an outlet of the water inlet pump, and a cold side outlet of the distilled water heater is connected with the non-condensable gas heater; the hot side inlet of the water cooler is connected with the outlet of the distilled water pump, and the hot side outlet of the water cooler is connected with the distilled water cooler;
the cold side inlet of the concentrated solution heater is connected with the other branch of the outlet of the water inlet pump; the hot side inlet of the device is connected with the outlet of the concentrated liquid pump, and the hot side outlet of the device is connected with the delivery pipeline;
a cold side inlet of the non-condensable gas heater is respectively connected with a cold side outlet of the distilled water heater and a cold side outlet of the concentrated solution heater, and a cold side outlet of the non-condensable gas heater is connected with an inlet of the forced circulation pump; the hot side inlet of the circulating evaporator is connected with the non-condensable gas outlet of the circulating evaporator separator;
the hot side inlet of the non-condensable gas cooler is connected with the hot side outlet of the non-condensable gas heater, and the hot side outlet of the non-condensable gas cooler is connected with the deodorization system; the inlet of the cold side of the cooling device is connected with circulating cooling water supply water, and the outlet of the cold side of the cooling device is connected with circulating cooling water outlet water;
the hot side inlet of the distilled water cooler is connected with the hot side outlet of the distilled water heater, and the hot side outlet is connected with the delivery pipeline; the inlet of the cold side of the cooling device is connected with circulating cooling water supply water, and the outlet of the cold side of the cooling device is connected with circulating cooling water outlet water;
the inlet of the distilled water tank is connected with the distilled water outlet of the shell-and-tube heat exchanger;
and the inlet of the distilled water pump is connected with the outlet of the distilled water tank, and the outlet of the distilled water pump is connected with the hot-side inlet of the distilled water heater.
The further effective effects are as follows: the heat can be fully recovered.
Further, the secondary steam purification system includes:
the horizontal pickling device is provided with a multi-stage spray chamber, and a secondary steam inlet of the horizontal pickling device is connected with a secondary steam outlet of the baffling type steam-liquid separator;
the horizontal alkali washing device is provided with a multi-stage spray chamber, a secondary steam inlet of the horizontal alkali washing device is connected with a secondary steam outlet of the horizontal acid washing device, and the secondary steam outlet is connected with an inlet of a steam compressor.
Further, an acid circulating spray pump is connected between a spray liquid outlet and a spray pipe inlet of each spray chamber of the horizontal pickling device;
and an alkali circulating spray pump is connected between a spray liquid outlet and a spray pipe inlet of each spray chamber of the horizontal alkali scrubber.
Adopt above-mentioned further beneficial effect to do: the multi-section secondary steam purification system is adopted, ammonia gas can instantly react with acid to generate ammonium sulfate salt such as sulfuric acid, most of organic matters can react with alkali to generate organic sodium salt such as sodium hydroxide according to the reaction principle, and the secondary steam purification system removes ammonia nitrogen and volatile organic matters in steam in a steam state stage by adopting the principle in a mode of connecting an acid washing steam chamber and an alkali washing steam chamber in series.
A high-concentration landfill leachate treatment process comprises the following steps:
s100, heating the high-concentration landfill leachate to be treated to 60-95 ℃ through a waste heat recovery system;
s200, allowing the heated high-concentration landfill leachate to flow into a pipe of a shell-and-tube heat exchanger through a forced circulation pump, and exchanging heat with secondary steam which is heated and pressurized by a steam compressor outside the pipe to enable the high-concentration landfill leachate to reach a boiling point;
s300, carrying out gas-liquid two-phase separation on the high-concentration landfill leachate reaching the boiling point in a chamber of a baffling type gas-liquid separator to obtain a liquid phase and secondary steam;
s400, sending the secondary steam separated by the baffling type steam-liquid separator into a secondary steam purification system to carry out acid washing and alkali washing in sequence;
s500, feeding the purified secondary steam into a vapor compressor to be heated and pressurized, returning the secondary steam to the outside of a shell-and-tube heat exchanger to be used as an evaporation heat source for heat exchange, condensing the secondary steam into distilled water, feeding the distilled water into a waste heat recovery system to recover and cool the distilled water, and discharging the distilled water;
and after mixing part of liquid phase in S600 and S300 with the high-concentration landfill leachate from the waste heat recovery system, sending the mixed liquid phase into a tube of a shell-and-tube heat exchanger through a forced circulation pump for heat exchange so as to raise the temperature to the boiling point again, then sending the mixed liquid phase into a chamber of a baffling type vapor-liquid separator for vapor-liquid separation, and sending part of liquid phase into the waste heat recovery system for waste heat recovery and then discharging.
Adopt above-mentioned further beneficial effect to do:
1) the process can ensure that the final produced water can reach the discharge standard specified in table 2 in the control standard for domestic refuse landfill GB 16889-2008;
2) the water yield (total water yield per day/total water inflow per day) of the process is 70-90%;
3) the process is provided with a waste heat recovery system, and meanwhile, the MVR process is adopted, so that the energy-saving effect is obvious;
4) the baffling type gas-liquid separator adopts a multi-stage separation principle, can effectively separate liquid drops in a gas phase, reduces pollutants to the rear end, and reduces acid-base washing load.
Further, the ratio of the flow rate of the high-concentration landfill leachate entering the waste heat recovery system to the flow rate of the forced circulation pump is 100-500.
Adopt above-mentioned further beneficial effect to do: the forced circulation process with high circulation ratio is adopted, the anti-scaling performance of the system is good, and the continuous stable operation period is longer than 20 days.
Further, the pressure of the secondary steam subjected to temperature rise and pressure rise is 50 kPaA-300 kPaA, and the temperature is 80-130 ℃; the boiling point temperature of the high-concentration landfill leachate is 75-125 ℃.
Further, the mass ratio of liquid to gas in the acid washing process is 10-200; the liquid-gas mass ratio in the alkali washing process is 20-350.
Drawings
FIG. 1 is a schematic diagram of a prior art MVR system;
fig. 2 is a layout diagram of the high-concentration landfill leachate treatment device in the invention.
In the drawings, the components represented by the respective reference numerals are listed below:
1. the system comprises a waste heat recovery system, a water inlet pump, a 120 concentrated liquid pump, a 130 distilled water heater, a 140 concentrated liquid heater, a 150 non-condensable gas heater, a 160 non-condensable gas cooler, a 170 distilled water cooler, a 180 distilled water tank, a 190 distilled water pump, a 2 MVR evaporation separation system, a 210 circulating evaporation separator, a 211, a shell-and-tube heat exchanger, a 212, a baffling type gas-liquid separator, a 220 forced circulation pump, a 230, a steam compressor, a 3, a secondary steam purification system, a 310, a horizontal acid pickling device, a 311, an acid circulating spray pump, a 320, a horizontal alkali washing device, a 321 and an alkali circulating spray pump.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention.
Example 1
As shown in fig. 2, a high concentration landfill leachate treatment device includes: the system comprises a waste heat recovery system 1, an MVR evaporation separation system 2 and a secondary steam purification system 3, wherein the waste heat recovery system 1 is connected with the MVR evaporation separation system 2, and the secondary steam purification system 3 is connected with the MVR evaporation separation system 2;
the MVR evaporative separation system 2 includes a cyclical evaporative separator 210 and a vapor compressor 230;
the circulating evaporation separator 210 comprises a shell-and-tube heat exchanger 211 and a baffled gas-liquid separator 212; generally, the shell-and-tube heat exchanger 211 and the baffled gas-liquid separator 212 are both horizontal structures; the tube pass of the shell-and-tube heat exchanger 211 can be designed into 1-20 tube passes according to actual project requirements, high-concentration landfill leachate flows in the tube, steam flows outside the tube, the high-concentration landfill leachate in the tube is heated by the steam outside the tube but is not evaporated, and the steam outside the tube transfers heat to the high-concentration landfill leachate and then turns into a liquid phase to form evaporation condensate;
the high-concentration landfill leachate after being heated in the waste heat recovery system 1 enters the pipe through a circulating liquid inlet of the shell-and-tube heat exchanger 211 and exchanges heat with steam outside the pipe so as to enable the high-concentration landfill leachate to reach a boiling point;
the baffling type vapor-liquid separator 212 is provided with a plurality of stages of chambers, wherein the first stage of chamber is a vapor-liquid two-phase separation chamber, and the other chambers are vapor-phase vapor-liquid deep separation and defoaming chambers; the outlet in the tube of the shell-and-tube heat exchanger 211 is connected with the vapor-liquid two-phase separation chamber; a secondary steam outlet of the steam phase vapor-liquid deep separation defoaming chamber at the last stage is connected with a secondary steam purification system 3; the purified secondary steam in the secondary steam purification system 3 is heated and pressurized by the steam compressor 230 and enters the outside of the tube of the shell-and-tube heat exchanger 211.
Example 2
As shown in fig. 2, this embodiment is further optimized based on embodiment 1, and it specifically includes the following steps:
the MVR evaporative separation system 2 further includes: and an inlet of the forced circulation pump 220 is connected with a high-concentration landfill leachate outlet of the waste heat recovery system 1, an outlet of the forced circulation pump 220 is connected with a circulating liquid inlet of the shell-and-tube heat exchanger 211, and a concentrated liquid outlet of the vapor-liquid two-phase separation chamber is communicated with an inlet of the forced circulation pump 220.
Example 3
As shown in fig. 2, this embodiment is further optimized based on embodiment 2, and the specific details thereof are as follows:
the waste heat recovery system 1 includes: a water inlet pump 110, a concentrated solution pump 120, a distilled water heater 130, a concentrated solution heater 140, a non-condensable gas heater 150, a non-condensable gas cooler 160, a distilled water cooler 170, a distilled water tank 180 and a distilled water pump 190;
the inlet of the water inlet pump 110 is externally connected with a high-concentration landfill leachate pipeline, and the outlet of the water inlet pump 110 is provided with two branches;
one branch of the outlet of the water inlet pump 110 is connected to the cold side inlet of the distilled water heater 130; the other branch of the inlet pump 110 outlet is connected to the cold side inlet of the concentrate heater 140;
a cold-side inlet of the distilled water heater 130 is connected with one branch of an outlet of the water inlet pump 110, and a cold-side outlet of the distilled water heater 130 is connected with the non-condensable gas heater 150; the hot side inlet of the distilled water heater 130 is connected with the outlet of the distilled water pump 190, and the hot side outlet of the distilled water heater 130 is connected with the distilled water cooler 170;
a distilled water outlet of the shell-and-tube heat exchanger 211 is connected with an inlet of the distilled water tank 180, an outlet of the distilled water tank 180 is connected with an inlet of the distilled water pump 190, an outlet of the distilled water pump 190 is connected with a hot side inlet of the distilled water heater 130, a hot side outlet of the distilled water heater 130 is connected with a hot side inlet of the distilled water cooler 170, and a hot side outlet of the distilled water cooler 170 is connected with an outgoing pipeline;
a non-condensable gas outlet of the shell-and-tube heat exchanger 211 is connected with a hot side inlet of the non-condensable gas heater 150, a hot side outlet of the non-condensable gas heater 150 is connected with a hot side inlet of the non-condensable gas cooler 160, and a hot side outlet of the non-condensable gas cooler 160 is connected with a deodorization system;
a concentrated solution outlet of a gas-liquid two-phase separation chamber in the baffling type gas-liquid separator 212 is connected with an inlet of a concentrated solution pump 120, an outlet of the concentrated solution pump 120 is connected with a hot side inlet of a concentrated solution heater 140, and a hot side outlet of the concentrated solution heater 140 is connected with an outward conveying pipeline;
the cold side inlet of the distilled water cooler 170 is connected with the circulating cooling water supply water, and the cold side outlet of the distilled water cooler 170 is connected with the circulating cooling water outlet water;
the cold side inlet of the non-condensable gas cooler 160 is connected with circulating cooling water supply water, and the cold side outlet of the non-condensable gas cooler 160 is connected with circulating cooling water outlet water.
Example 4
As shown in fig. 2, this embodiment is further optimized based on embodiment 2, and the specific details thereof are as follows:
the secondary steam purification system 3 includes: a horizontal acid washer 310 and a horizontal caustic washer 320;
the horizontal acid washer 310 has a multi-stage spray chamber, and the horizontal alkali washer 320 has a multi-stage spray chamber;
the secondary steam inlet of the horizontal pickling device 310 is connected with the secondary steam outlet of the baffling type steam-liquid separator 212; the secondary steam inlet of the horizontal alkaline cleaner 320 is connected with the secondary steam outlet of the horizontal acid cleaner 310, and the secondary steam outlet of the horizontal alkaline cleaner 320 is connected with the inlet of the steam compressor 230.
Example 5
As shown in fig. 2, this embodiment is further optimized based on embodiment 4, and the details thereof are as follows:
an acid circulating spray pump 311 is connected between a spray liquid outlet and a spray pipe inlet of each spray chamber of the horizontal pickling device 310;
in this embodiment, the horizontal pickling device 310 has a three-stage spray chamber, and mainly removes ammonia nitrogen pollutants in the steam after pickling; an alkali circulation spray pump 321 is connected between a spray liquid outlet and a spray pipe inlet of each spray chamber of the horizontal alkali scrubber 320; (ii) a
In this embodiment, the horizontal alkaline scrubber 320 has a three-stage spray chamber, and mainly removes organic matters in steam through alkaline scrubbing;
the mass ratio of liquid to gas in the acid washing process is 10-200, and the mass ratio of liquid to gas in the alkali washing process is 20-350.
Example 6
A high-concentration landfill leachate treatment process comprises the following steps:
s100, enabling high-concentration landfill leachate to be treated to enter a distilled water heater 130 and a concentrated solution heater 140 for heat exchange in two ways through a water inlet pump 110, then combining the two ways into one way, and then entering a non-condensable gas heater 150 for heat exchange to realize that the high-concentration landfill leachate is heated to 60-95 ℃;
s200, enabling the high-concentration landfill leachate heated by the distilled water heater 130, the concentrated solution heater 140 and the non-condensable gas heater 150 to flow into a pipe of a shell-and-tube heat exchanger 211 through a forced circulation pump 220, and exchanging heat with secondary steam which is heated and pressurized by a steam compressor 230 outside the pipe to enable the high-concentration landfill leachate to reach a boiling point;
s300, carrying out vapor-liquid two-phase separation on the high-concentration landfill leachate reaching the boiling point in a vapor-liquid two-phase separation chamber of the baffled vapor-liquid separator 212, and further separating liquid drops in the gas phase through a subsequent other vapor-phase vapor-liquid deep separation defoaming chamber to finally obtain a liquid phase and secondary steam;
s400, sending the secondary steam separated by the baffling type steam-liquid separator 212 into a secondary steam purification system 3 for acid washing and alkali washing in sequence;
s500, feeding the purified secondary steam into a vapor compressor 230 to be heated and pressurized, returning the secondary steam to the outside of a shell-and-tube heat exchanger 211 to be used as an evaporation heat source for heat exchange, condensing the secondary steam into distilled water, feeding the distilled water into a distilled water tank 180, feeding the distilled water into a waste heat recovery system 1 to recover and cool the waste heat, and discharging the distilled water;
s600, after mixing the partial liquid phase in the S300 with the high-concentration landfill leachate from the waste heat recovery system 1, sending the mixed liquid phase into the tube of the shell-and-tube heat exchanger 211 through the forced circulation pump 220 for heat exchange, heating the mixed liquid phase to the boiling point again, then sending the mixed liquid phase into the chamber of the baffling type gas-liquid separator 212 for gas-liquid separation, and sending the partial liquid phase into the waste heat recovery system 1 for waste heat recovery and then discharging the separated liquid phase.
Example 7
This example is a further optimization performed on the basis of example 6, and it is specifically as follows:
the ratio of the flow of the high-concentration landfill leachate entering the waste heat recovery system 1 to the flow of the forced circulation pump 220 is 100-500, namely the ratio of the flow of the water inlet pump 110 to the flow of the forced circulation pump 220 is 100-500, so that the scaling tendency of the heating section can be reduced.
Example 8
This example is a further optimization performed on the basis of example 6 or 7, and is specifically as follows:
the pressure of the secondary steam after temperature rise and pressure rise is 50 kPaA-300 kPaA, and the temperature is 80-130 ℃; the boiling point temperature of the high-concentration landfill leachate is 75-125 ℃;
the waste heat recovery system 1 recovers heat of high-temperature MVR concentrated solution (80-120 ℃) and high-temperature distilled water (80-105 ℃) discharged by the MVR evaporation separation system 2, the recovered heat heats high-concentration landfill leachate sent into the process system by the water inlet pump 110 to 60-95 ℃, and the high-temperature distilled water recovered by the waste heat is further reduced to 35-55 ℃ by circulating cooling water and discharged.
Example 9
This example is a further optimization based on example 6, 7 or 8, which is specifically as follows:
the mass ratio of liquid to gas in the acid washing process is 10-200; the liquid-gas mass ratio in the alkali washing process is 20-350.
In the invention, the typical pollutant range in the high-concentration landfill leachate is COD (chemical oxygen demand) 5000 mg/l-50000 mg/l and NH3-N:500mg/l～10000mg/l，TDS:5000mg/l～100000mg/l。
The process can ensure that the final produced water can reach the discharge standard specified in table 2 in the control standard for domestic refuse landfill GB 16889-2008.
The water yield (total daily water yield/total daily water inflow) of the process is 70-90%.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (10)
1. The utility model provides a high enriched landfill leachate processing apparatus which characterized in that includes: the system comprises a waste heat recovery system (1), an MVR evaporation separation system (2) and a secondary steam purification system (3); the MVR evaporative separation system (2) comprises a circulating evaporative separator (210) and a vapor compressor (230); the circulating evaporation separator (210) comprises a shell-and-tube heat exchanger (211) and a baffled gas-liquid separator (212); the high-concentration landfill leachate after being heated in the waste heat recovery system (1) enters the pipe through a circulating liquid inlet of the shell-and-tube heat exchanger (211) and exchanges heat with steam outside the pipe so as to enable the high-concentration landfill leachate to reach a boiling point; the baffling type vapor-liquid separator (212) is provided with a plurality of stages of chambers, the first stage of chamber is a vapor-liquid two-phase separation chamber, and the other chambers are vapor-phase vapor-liquid deep separation and defoaming chambers; an outlet in the tube of the shell-and-tube heat exchanger (211) is connected with the vapor-liquid two-phase separation chamber; a secondary steam outlet of the steam phase vapor-liquid deep separation defoaming chamber at the last stage is connected with a secondary steam purification system (3); the secondary steam purified in the secondary steam purification system (3) is heated and pressurized by a steam compressor (230) and then enters the outside of the tube of the shell-and-tube heat exchanger (211).
2. The high-concentration landfill leachate treatment device according to claim 1, wherein: the MVR evaporative separation system (2) further comprises:
and an inlet of the forced circulation pump (220) is connected with a high-concentration landfill leachate liquid outlet of the waste heat recovery system (1), and an outlet of the forced circulation pump is connected with a circulation liquid inlet of the shell-and-tube heat exchanger (211).
3. The high-concentration landfill leachate treatment device according to claim 1 or 2, wherein: and a concentrated solution outlet of the vapor-liquid two-phase separation chamber is communicated with an inlet of a forced circulation pump (220).
4. The high-concentration landfill leachate treatment plant according to claim 1, 2 or 3, wherein: the waste heat recovery system (1) comprises:
the inlet of the water inlet pump (110) is externally connected with a high-concentration landfill leachate pipeline, and the outlet of the water inlet pump is provided with two branches;
a concentrated liquid pump (120), the inlet of which is connected with the concentrated liquid outlet of the vapor-liquid two-phase separation chamber, and the outlet of which is connected with an outward pipeline;
the cold side inlet of the distilled water heater (130) is connected with one branch of the outlet of the water inlet pump (110), and the cold side outlet is connected with the non-condensable gas heater (150); the hot side inlet of the water cooler is connected with the outlet of the distilled water pump (190), and the hot side outlet of the water cooler is connected with the distilled water cooler (170);
a concentrated solution heater (140), wherein the cold side inlet of the concentrated solution heater is connected with the other branch of the outlet of the water inlet pump (110); the hot side inlet of the device is connected with the outlet of a concentrated liquid pump (120), and the hot side outlet is connected with an outward conveying pipeline;
a non-condensable gas heater (150), wherein a cold side inlet of the non-condensable gas heater is respectively connected with a cold side outlet of the distilled water heater (130) and a cold side outlet of the concentrated solution heater (140), and a cold side outlet of the non-condensable gas heater is connected with an inlet of the forced circulation pump (220); the hot side inlet of the circulating evaporator is connected with the non-condensable gas outlet of the circulating evaporator separator (210);
the non-condensable gas cooler (160), its hot side inlet is connected with hot side outlet of the non-condensable gas heater (150), its hot side outlet is connected with deodorizing system; the inlet of the cold side of the cooling device is connected with circulating cooling water supply water, and the outlet of the cold side of the cooling device is connected with circulating cooling water outlet water;
the hot side inlet of the distilled water cooler (170) is connected with the hot side outlet of the distilled water heater (130), and the hot side outlet is connected with the delivery pipeline; the inlet of the cold side of the cooling device is connected with circulating cooling water supply water, and the outlet of the cold side of the cooling device is connected with circulating cooling water outlet water;
a distilled water tank (180) having an inlet connected to a distilled water outlet of the shell-and-tube heat exchanger (211);
and the inlet of the distilled water pump (190) is connected with the outlet of the distilled water tank (180), and the outlet is connected with the hot side inlet of the distilled water heater (130).
5. The high-concentration landfill leachate treatment process according to claim 4, wherein the treatment process comprises the following steps: the secondary steam purification system (3) comprises:
the horizontal pickling device (310) is provided with a multi-stage spray chamber, and a secondary steam inlet of the horizontal pickling device is connected with a secondary steam outlet of the baffling type steam-liquid separator (212);
the horizontal alkaline cleaner (320) is provided with a multi-stage spray chamber, a secondary steam inlet of the horizontal alkaline cleaner is connected with a secondary steam outlet of the horizontal acid cleaner (310), and the secondary steam outlet is connected with an inlet of the steam compressor (230).
6. The high-concentration landfill leachate treatment process according to claim 5, wherein the treatment process comprises the following steps:
an acid circulating spray pump (311) is connected between a spray liquid outlet and a spray pipe inlet of each spray chamber of the horizontal pickling device (310);
and an alkali circulating spray pump (321) is connected between a spray liquid outlet and a spray pipe inlet of each spray chamber of the horizontal alkali scrubber (320).
7. A high-concentration landfill leachate treatment process is characterized by comprising the following steps:
s100, heating the high-concentration landfill leachate to be treated to 60-95 ℃ through a waste heat recovery system (1);
s200, the heated high-concentration landfill leachate flows into a pipe of a shell-and-tube heat exchanger (211) through a forced circulation pump (220), and exchanges heat with secondary steam which is heated and pressurized by a steam compressor (230) outside the pipe, so that the high-concentration landfill leachate reaches a boiling point;
s300, carrying out gas-liquid two-phase separation on the high-concentration landfill leachate reaching the boiling point in a chamber of a baffling type gas-liquid separator (212) to obtain a liquid phase and secondary steam;
s400, sending the secondary steam separated by the baffling type steam-liquid separator (212) into a secondary steam purification system (3) for acid washing and alkali washing in sequence;
s500, feeding the purified secondary steam into a vapor compressor (230) to be heated and boosted, returning the secondary steam to the outside of a shell-and-tube heat exchanger (211) to be used as an evaporation heat source for heat exchange, condensing the secondary steam into distilled water, feeding the distilled water into a waste heat recovery system (1), recovering waste heat, cooling and discharging;
s600, after mixing part of liquid phase in the S300 with high-concentration landfill leachate from the waste heat recovery system (1), sending the mixed liquid into a tube of a shell-and-tube heat exchanger (211) through a forced circulation pump (220) for heat exchange so as to raise the temperature to the boiling point again, then entering a chamber of a baffling type vapor-liquid separator (212) for vapor-liquid separation, and sending part of liquid phase into the waste heat recovery system (1) for waste heat recovery and then discharging.
8. The high-concentration landfill leachate treatment process according to claim 7, wherein the ratio of the flow rate of the high-concentration landfill leachate entering the waste heat recovery system (1) to the flow rate of the forced circulation pump (220) is 100-500.
9. The process for treating high-concentration landfill leachate according to claim 7, wherein the pressure of the secondary steam with increased temperature and pressure is 50kPaA to 300kPaA, and the temperature is 80 ℃ to 130 ℃; the boiling point temperature of the high-concentration landfill leachate is 75-125 ℃.
10. The treatment process of high-concentration landfill leachate according to claim 7, wherein the liquid-gas mass ratio in the acid washing process is 10 to 200; the liquid-gas mass ratio in the alkali washing process is 20-350.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111057201.1A CN113880166A (en) | 2021-09-09 | 2021-09-09 | High-concentration landfill leachate treatment process and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111057201.1A CN113880166A (en) | 2021-09-09 | 2021-09-09 | High-concentration landfill leachate treatment process and device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113880166A true CN113880166A (en) | 2022-01-04 |
Family
ID=79008545
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111057201.1A Pending CN113880166A (en) | 2021-09-09 | 2021-09-09 | High-concentration landfill leachate treatment process and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113880166A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114804476A (en) * | 2022-03-28 | 2022-07-29 | 武汉天源环保股份有限公司 | Landfill leachate treatment system and treatment method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204588908U (en) * | 2015-04-30 | 2015-08-26 | 中山中珠环保科技有限公司 | A kind of New-type refuse vehicle percolation liquid treating system |
| CN205740622U (en) * | 2016-06-15 | 2016-11-30 | 广州市迈源科技有限责任公司 | A kind of percolate coagulating sedimentation, evaporation joint processing system |
| WO2017124215A1 (en) * | 2016-01-18 | 2017-07-27 | 江门市佰川环境科技有限公司 | Double-effect cross-flow mvr evaporation concentration system |
| CN111547799A (en) * | 2020-06-27 | 2020-08-18 | 商洛市海蓝科技有限公司 | Low-temperature evaporation treatment system for wastewater and landfill leachate |
| CN112390426A (en) * | 2020-10-09 | 2021-02-23 | 武汉泾渭环境科技有限公司 | Landfill leachate ammonia nitrogen removal method |
| CN112624475A (en) * | 2020-12-21 | 2021-04-09 | 大连广泰源环保科技有限公司 | Zero-discharge treatment system and process for landfill leachate |
-
2021
- 2021-09-09 CN CN202111057201.1A patent/CN113880166A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204588908U (en) * | 2015-04-30 | 2015-08-26 | 中山中珠环保科技有限公司 | A kind of New-type refuse vehicle percolation liquid treating system |
| WO2017124215A1 (en) * | 2016-01-18 | 2017-07-27 | 江门市佰川环境科技有限公司 | Double-effect cross-flow mvr evaporation concentration system |
| CN205740622U (en) * | 2016-06-15 | 2016-11-30 | 广州市迈源科技有限责任公司 | A kind of percolate coagulating sedimentation, evaporation joint processing system |
| CN111547799A (en) * | 2020-06-27 | 2020-08-18 | 商洛市海蓝科技有限公司 | Low-temperature evaporation treatment system for wastewater and landfill leachate |
| CN112390426A (en) * | 2020-10-09 | 2021-02-23 | 武汉泾渭环境科技有限公司 | Landfill leachate ammonia nitrogen removal method |
| CN112624475A (en) * | 2020-12-21 | 2021-04-09 | 大连广泰源环保科技有限公司 | Zero-discharge treatment system and process for landfill leachate |
Non-Patent Citations (1)
| Title |
|---|
| 《化学工程手册》编辑委员会: "《热传递理论、实践与应用》", 哈尔滨工业大学出版社, pages: 336 - 337 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114804476A (en) * | 2022-03-28 | 2022-07-29 | 武汉天源环保股份有限公司 | Landfill leachate treatment system and treatment method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| WO2022126671A1 (en) | Water treatment device for concentrating, crystallizing and desalting high-salinity wastewater by means of lithium bromide unit | |
| CN105366867A (en) | Single-effect multi-chamber mechanical compression evaporation device for processing high-salinity/high-organic-substance-content wastewater and method thereof | |
| CN111115735A (en) | Two-stage forced circulation evaporation system and process for landfill leachate | |
| CN108751302A (en) | A kind of vacuum and low temperature evaporating separation device and sewage water treatment method | |
| WO2022041476A1 (en) | Salt-containing wastewater treatment apparatus | |
| CN216073129U (en) | High-concentration landfill leachate treatment device | |
| CN113735209A (en) | Full-quantification landfill leachate treatment device and process | |
| CN113880166A (en) | High-concentration landfill leachate treatment process and device | |
| WO2022126670A1 (en) | Salt-containing water desalination treatment device for concentrating and crystallizing high-salt wastewater by means of heat pump | |
| CN215905885U (en) | Full-quantification landfill leachate treatment device | |
| CN112875968A (en) | Desulfurization wastewater zero discharge system and method thereof | |
| CN105091409A (en) | Straight-through type heat pump | |
| CN209635926U (en) | Falling film evaporation couples absorption refrigeration high-salt sewage processing equipment | |
| CN216808187U (en) | Separation tower for treating condensed water | |
| CN210645170U (en) | Double-effect external circulation evaporator | |
| CN216295220U (en) | MVR evaporation concentration system for processing emulsion | |
| CN110404281A (en) | A kind of economic benefits and social benefits external circulation evaporator | |
| CN211871447U (en) | Two-stage forced circulation evaporation system for landfill leachate | |
| CN210855354U (en) | Multistage evaporating system of low temperature low pressure high concentration salt waste water zero release | |
| CN111517400B (en) | Low-grade heat source coupling multi-effect flash evaporation concentration evaporation system | |
| CN110697814B (en) | Ammonia-containing sulfate wastewater treatment system and process | |
| CN211921179U (en) | Power plant wet desulphurization wastewater zero discharge system | |
| CN111320220A (en) | Process and device for concentrating high-salinity wastewater by circularly stripping air or industrial gas | |
| CN112142246A (en) | High-salt high-organic-matter wastewater zero-discharge treatment process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |