CN106865860A - Energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit and method of wastewater treatment - Google Patents
Energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit and method of wastewater treatment Download PDFInfo
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- CN106865860A CN106865860A CN201710164498.9A CN201710164498A CN106865860A CN 106865860 A CN106865860 A CN 106865860A CN 201710164498 A CN201710164498 A CN 201710164498A CN 106865860 A CN106865860 A CN 106865860A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 25
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 22
- 230000003647 oxidation Effects 0.000 title claims abstract description 17
- 238000011084 recovery Methods 0.000 title claims abstract description 16
- 238000004065 wastewater treatment Methods 0.000 title claims description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 130
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 82
- 239000007788 liquid Substances 0.000 claims abstract description 58
- 230000008676 import Effects 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 24
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- 239000007791 liquid phase Substances 0.000 claims abstract description 22
- 239000006096 absorbing agent Substances 0.000 claims abstract description 10
- 239000007792 gaseous phase Substances 0.000 claims abstract description 8
- 238000003860 storage Methods 0.000 claims abstract description 8
- 239000002815 homogeneous catalyst Substances 0.000 claims description 37
- 238000007599 discharging Methods 0.000 claims description 16
- 150000003839 salts Chemical class 0.000 claims description 16
- 239000012071 phase Substances 0.000 claims description 14
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- 239000012452 mother liquor Substances 0.000 claims description 10
- 238000007172 homogeneous catalysis Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 8
- 238000007210 heterogeneous catalysis Methods 0.000 claims description 8
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical compound [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 8
- 238000009279 wet oxidation reaction Methods 0.000 claims description 8
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Chemical compound [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 claims description 8
- 238000001704 evaporation Methods 0.000 claims description 7
- 239000002638 heterogeneous catalyst Substances 0.000 claims description 7
- 238000010025 steaming Methods 0.000 claims description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 239000004408 titanium dioxide Substances 0.000 claims description 6
- 229910052684 Cerium Inorganic materials 0.000 claims description 4
- 229910052779 Neodymium Inorganic materials 0.000 claims description 4
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 4
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 4
- 230000002411 adverse Effects 0.000 claims description 4
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 4
- KTVIXTQDYHMGHF-UHFFFAOYSA-L cobalt(2+) sulfate Chemical compound [Co+2].[O-]S([O-])(=O)=O KTVIXTQDYHMGHF-UHFFFAOYSA-L 0.000 claims description 4
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 claims description 4
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 229910052746 lanthanum Inorganic materials 0.000 claims description 4
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 claims description 4
- 229940099596 manganese sulfate Drugs 0.000 claims description 4
- 235000007079 manganese sulphate Nutrition 0.000 claims description 4
- 239000011702 manganese sulphate Substances 0.000 claims description 4
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(2+);dinitrate Chemical compound [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 claims description 4
- SQQMAOCOWKFBNP-UHFFFAOYSA-L manganese(II) sulfate Chemical compound [Mn+2].[O-]S([O-])(=O)=O SQQMAOCOWKFBNP-UHFFFAOYSA-L 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- QEFYFXOXNSNQGX-UHFFFAOYSA-N neodymium atom Chemical compound [Nd] QEFYFXOXNSNQGX-UHFFFAOYSA-N 0.000 claims description 4
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 claims description 4
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 claims description 4
- 229910052763 palladium Inorganic materials 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- 229910052703 rhodium Inorganic materials 0.000 claims description 4
- 239000010948 rhodium Substances 0.000 claims description 4
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 4
- 229910052707 ruthenium Inorganic materials 0.000 claims description 4
- 229910052709 silver Inorganic materials 0.000 claims description 4
- 239000004332 silver Substances 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 claims description 4
- 229910000368 zinc sulfate Inorganic materials 0.000 claims description 4
- 229960001763 zinc sulfate Drugs 0.000 claims description 4
- 229910017052 cobalt Inorganic materials 0.000 claims description 3
- 239000010941 cobalt Substances 0.000 claims description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 3
- 238000002425 crystallisation Methods 0.000 claims description 3
- 230000008025 crystallization Effects 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical group [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 3
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 claims description 3
- 229910000510 noble metal Inorganic materials 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 2
- 229910017604 nitric acid Inorganic materials 0.000 claims description 2
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 claims description 2
- 238000010992 reflux Methods 0.000 claims description 2
- 239000012876 carrier material Substances 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 7
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000010815 organic waste Substances 0.000 description 10
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 239000012528 membrane Substances 0.000 description 6
- 239000002918 waste heat Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 4
- 229910052593 corundum Inorganic materials 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000003911 water pollution Methods 0.000 description 3
- 229910001845 yogo sapphire Inorganic materials 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 2
- -1 bio-toxicity is big Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 229910052726 zirconium Inorganic materials 0.000 description 2
- FGRBYDKOBBBPOI-UHFFFAOYSA-N 10,10-dioxo-2-[4-(N-phenylanilino)phenyl]thioxanthen-9-one Chemical compound O=C1c2ccccc2S(=O)(=O)c2ccc(cc12)-c1ccc(cc1)N(c1ccccc1)c1ccccc1 FGRBYDKOBBBPOI-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 1
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 1
- HJSLFCCWAKVHIW-UHFFFAOYSA-N cyclohexane-1,3-dione Chemical compound O=C1CCCC(=O)C1 HJSLFCCWAKVHIW-UHFFFAOYSA-N 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- MVZXTUSAYBWAAM-UHFFFAOYSA-N iron;sulfuric acid Chemical group [Fe].OS(O)(=O)=O MVZXTUSAYBWAAM-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a kind of energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit, waste water storage tank connects First Heat Exchanger simultaneously with catalyst carrier, First Heat Exchanger connects the first reaction tower, first reaction tower connects the second heat exchanger, second heat exchanger connects the second reaction tower, the heat exchange water out connection turbine generators of the second heat exchanger, second reaction tower connects the first gas-liquid separator, the gaseous phase outlet of the first gas-liquid separator is communicated with the first tail gas absorber, liquid-phase outlet is communicated with MVR evaporators, MVR evaporators connect the 3rd heat exchanger, 3rd heat exchanger connects the 3rd reaction tower, 3rd reaction tower connects the second gas-liquid separator, the gaseous phase outlet of the second gas-liquid separator connects the import of the second tail gas absorber；Air compressor machine is the first reaction tower, the second reaction tower and the 3rd reaction tower provide reaction air.The method have the advantages that：High concentration high salinity waste water can directly be processed, environmental protection, low cost, effect is good, floor space is small, recoverable energy.
Description
Technical field
The present invention relates to a kind of industrial organic waste water processing technology field, and in particular to one kind is used to process that high concentration is high to be contained
The apparatus and method of salt industrial organic wastewater.
Background technology
Water pollution is the major issue that a China needs to address at present.Solving water pollution problems should just solve first
The generation in the source certainly polluted, i.e. sewage and discharge, and the industrial organic waste water that factory produces be water pollution main source it
One.Pollutant component is complicated in industrial wastewater, bio-toxicity is big, COD is high, salinity is high, color is deep, taste weight, processes very tired
It is difficult.Processing method main at present has：Bioanalysis, extraction, burning method, Fenton process and Ozone etc., but these methods lack
Putting is：（1）Processing cost is high and poor processing effect；（2）COD contents cannot directly be processed more than 100,000 mg/L and high salinity
Waste water, before high slat-containing wastewater is processed, it is necessary to which first diluting the COD contents and salt content of high concentration high slat-containing wastewater reduces, place
Reason step complexity is cumbersome；（3）The occupation area of equipment applied is big；（4）Exist to the secondary of environment in wastewater treatment process
Pollution and a large amount of wastes of energy, not energy-conserving and environment-protective.
The content of the invention
Can directly and efficiently process high concentration highly salt containing organic waste water it is an object of the invention to provide one kind, in waste water
The energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit of non-secondary pollution and energy effective recycling energy in processing procedure
And method of wastewater treatment.
To achieve the above object, present invention employs following technical scheme：A kind of described energy recovery type waste water catalysis
Wet oxidation processing unit, including be used to store the waste water storage tank of waste water, be used to store the catalyst carrier of catalyst, Yi Jikong
Press, the delivery port of the waste water storage tank is communicated with the charging aperture of First Heat Exchanger simultaneously with the discharging opening of catalyst carrier, the
The discharging opening of one heat exchanger is communicated with the import of the first reaction tower, the first reaction tower outlet and the second heat exchanger charging aperture phase
Logical, the discharging opening of the second heat exchanger is communicated with the import of the second reaction tower, and the heat exchange water out connection of second heat exchanger is saturating
Flat generator, the outlet of second reaction tower is connected through First Heat Exchanger with the import of the first gas-liquid separator, the first gas
The gaseous phase outlet of liquid/gas separator is connected with the import of the first tail gas absorber, the liquid-phase outlet and MVR of the first gas-liquid separator
The charging aperture of evaporator is connected, and the condensation-water drain of MVR evaporators is connected with the charging aperture of the 3rd heat exchanger, the 3rd heat exchange
The discharging opening of device is connected with the import of the 3rd reaction tower, and the outlet of the 3rd reaction tower is through the 3rd heat exchanger and the second gas-liquid separation
The import of device is connected, and the gaseous phase outlet of the second gas-liquid separator is connected with the import of the second tail gas absorber；The pneumatics
Machine is by pipeline simultaneously for the first reaction tower, the second reaction tower and the 3rd reaction tower carry available for reaction air.
Further, foregoing a kind of energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit, wherein：Second reaction tower
Outlet be connected with the shell of First Heat Exchanger, cold material and thermal material adverse current by First Heat Exchanger, First Heat Exchanger
Shell outlet is connected with the import of the first gas-liquid separator.
Further, foregoing a kind of energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit, wherein：3rd reaction tower
Outlet be connected with the shell of the 3rd heat exchanger, cold material and thermal material adverse current by the 3rd heat exchanger, the 3rd heat exchanger
Shell outlet is connected with the import of the second gas-liquid separator.
Further, foregoing a kind of energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit, wherein：First gas-liquid point
Liquid-phase outlet from device is connected with the charging aperture of the first dashpot, the discharging opening of the first dashpot and the charging of MVR evaporators
Mouth is connected.
Further, foregoing a kind of energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit, wherein：MVR evaporators
Steaming more than mother liquor reflux to catalyst carrier.
A kind of method of wastewater treatment, comprises the following steps：
（1）Heated up again after first homogeneous catalyst is mixed with waste water and be passed through the first reaction tower, be mixed with homogeneous catalyst waste water and
The reaction provided by air compressor machine in first reaction tower carries out first time homogeneous catalysis wet type in the first reaction tower together with air
Oxidation reaction, first road treatment water of the generation comprising homogeneous catalyst；
（2）Then by step（1）The second reaction tower is passed through after the first road treatment water cooling of generation, then Shi Chu roads treatment water and the
The reaction provided by air compressor machine in two reaction towers carries out second homogeneous catalysis wet type oxygen with air in the second reaction tower together
Change reaction, two roads treatment water of the generation comprising homogeneous catalyst；
（3）Then by step（2）Being passed through the first gas-liquid separator after the two roads treatment water cooling of generation carries out gas-liquid separation, generates
Gas phase and the liquid phase containing homogeneous catalyst；
（4）Then by step（3）The liquid phase of generation is passed through MVR evaporators and is evaporated, and generates colourless crystallization salt, condensed water and contains
There is mother liquor more than the steaming of homogeneous catalyst；
（5）Then by step（4）The condensed water of generation is passed through the 3rd reaction tower, multiphase in condensed water and the 3rd reaction tower after heating up
Catalyst and by air compressor machine provide reaction carry out heterogeneous catalysis wet oxidation reaction in the 3rd reaction tower together with air,
Generate three roads treatment water；
（6）Then by step（5）Being passed through the second gas-liquid separator after the three roads treatment water cooling of generation carries out gas-liquid separation, generates
Gas phase and meet the liquid phase of discharge standard.
Described homogeneous catalyst is ferric sulfate, ferric nitrate, copper sulphate, copper nitrate, manganese sulfate, manganese nitrate, cobaltous sulfate, nitre
One or more in sour cobalt, zinc sulfate, zinc nitrate, nickel sulfate, nickel nitrate.
Described heterogeneous catalyst is noble metal carrier catalyst, and its carrier is activated carbon, titanium dioxide, titanium dioxide
One or more in zirconium, alundum (Al2O3), silica and molecular sieve combination, its active component be ruthenium, rhodium, palladium, silver, platinum,
One or more in cerium, lanthanum, neodymium.
Further, foregoing a kind of method of wastewater treatment, wherein：Step（1）Middle Characteristic of Homogenous Catalytic Wet Air Oxidation reaction
Reaction condition is：Reaction temperature is（250~300）DEG C, reaction pressure is（4.5~9）MPa, liquid hourly space velocity (LHSV) is（0.5~3） h-1,
The dosage of wherein homogeneous catalyst is that every liter of waste water is added（50~500）mg（With metal ion gauge）.
Further, foregoing a kind of method of wastewater treatment, wherein：Step（2）Middle Characteristic of Homogenous Catalytic Wet Air Oxidation reaction
Reaction condition is：Reaction temperature is（220~290）DEG C, reaction pressure is（2.5~8）MPa, liquid hourly space velocity (LHSV) is（0.5~3） h-1,
The dosage of wherein homogeneous catalyst is that every liter of waste water is added（50~500）mg（With metal ion gauge）.
Further, foregoing a kind of method of wastewater treatment, wherein：Step（4）The evaporation conditionses of middle MVR evaporators are：
Evaporating temperature is（50~100）DEG C, remaining mother liquor amount control is steamed in step（3）The amount of liquid phase of generation（1~10）%.
Further, foregoing a kind of method of wastewater treatment, wherein：Step（5）Middle heterogeneous catalysis wet oxidation reaction
Reaction condition is：Reaction temperature is（180~280）DEG C, reaction pressure is（2.0~7.5）MPa, liquid hourly space velocity (LHSV) is（0.5~3） h-1。
By the implementation of above-mentioned technical proposal, the advantage of wastewater treatment equipment of the present invention is：（1）Processing cost is low, treatment
Effect is good, floor space is small and high degree of automation；（2）Waste water need not be diluted, it is possible to directly process COD contents more than 100,000
The waste water of mg/L and high salinity；（3）In the absence of the secondary pollution to environment in wastewater treatment process；（4）By heat exchanger
Waste heat is reclaimed, and the steam that heat exchanger is produced generates electricity for turbine generators, has reached the purpose that energy regenerating is utilized,
Not only realize environmental benefit but also obtain economic benefit；The advantage of method of wastewater treatment of the present invention is：Good treatment efficiency, COD clearances
Height, COD clearances are more than 95.5%, in the absence of the secondary pollution to environment in wastewater treatment process and useless without dilution
Water, it is possible to directly process COD contents more than 100,000 mg/L and the waste water of high salinity, it is especially volatile to treatment organic principle
Waste water have more advantage, MVR steams the reuse of remaining mother liquor and prepares that homogeneous catalyst had not only solved the problems, such as concentrate and to reach circulation sharp
Purpose, and salt is separated out for colourless clean salt, recyclable recycling.
Brief description of the drawings
Fig. 1 is that a kind of structural principle of energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit of the present invention is illustrated
Figure.
Specific embodiment
The invention will be further described with specific embodiment below in conjunction with the accompanying drawings.
As shown in figure 1, a kind of described energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit, including be used to store useless
The waste water storage tank 1 of water, it is used to store the catalyst carrier 2 and air compressor machine 3 of catalyst, the delivery port of the waste water storage tank 1 leads to
Cross and be provided with the first pipeline 5 of the first membrane pump 4 and be connected with the import of pipe-line mixer 6, the discharging opening of catalyst carrier 2 passes through
Second pipeline 7 is connected with the import of pipe-line mixer 6, the outlet of pipe-line mixer 6 and the charging aperture phase of First Heat Exchanger 9
Logical, the discharging opening of First Heat Exchanger 9 is communicated with the import of the first reaction tower 10, and the outlet at the top of the first reaction tower 10 passes through the 4th
Pipeline 12 is communicated with the charging aperture of the second heat exchanger 11, the import phase of the discharging opening of the second heat exchanger 11 and the second reaction tower 13
It is logical, the heat exchange water out connection turbine generators 14 of the second heat exchanger 11, the top exit of the second reaction tower 13 is by the 5th pipe
Road 15 is connected with the heat exchange water inlet of First Heat Exchanger 9, and the heat exchange water out of First Heat Exchanger 9 is by the 6th pipeline 16 and the
The import of one gas-liquid separator 17 is connected, and two roads that the second reaction tower 13 can so generated process the waste heat pair of water
Heat temperature raising is carried out by the high concentration highly salt containing organic waste water of First Heat Exchanger 9, homogeneous catalyst and air three mixture,
So as to reclaim heat, the energy has been saved；
The gaseous phase outlet of the first gas-liquid separator 17 is connected by the 7th pipeline 18 with the import of the first tail gas absorber 19, the
The liquid-phase outlet of one gas-liquid separator 17 is connected by the 8th pipeline 20 with the charging aperture of the first dashpot 21, the first dashpot
21 discharging opening is connected by being provided with the 9th pipeline 23 of the second membrane pump 22 with the charging aperture of MVR evaporators 24, MVR evaporations
The condensation-water drain of device 24 is connected by being provided with the tenth pipeline 26 of the 3rd membrane pump 25 with the charging aperture of the 3rd heat exchanger 27,
The discharging opening of the 3rd heat exchanger 27 is connected with the import of the 3rd reaction tower 28, and the top exit of the 3rd reaction tower 28 passes through the tenth
One pipeline 29 is connected with the heat exchange water inlet of the 3rd heat exchanger 27, and the heat exchange water out of the 3rd heat exchanger 27 is by the 12nd pipe
Road 30 is connected with the import of the second gas-liquid separator 31, and three roads that the 3rd reaction tower 28 can so generated process many of water
Waste heat amount carries out heat temperature raising to the condensed water by the 3rd heat exchanger 27, so as to reclaim heat, has saved the energy；
The gaseous phase outlet of the second gas-liquid separator 31 is connected by the 13rd pipeline 32 with the import of the second tail gas absorber 33,
The liquid-phase outlet of the second gas-liquid separator 31 is connected by the 14th pipeline 34 with the charging aperture of the second dashpot 35；The sky
Press 3 is connected by the 3rd pipeline 8 with the import of pipe-line mixer 6, so that for the first reaction tower 10 carries available for reaction air,
And by the 15th pipeline 36 that is connected with the 4th pipeline 12 for the second reaction tower 13 carries available for reaction air, while passing through
The 16th pipeline 37 being connected with the tenth pipeline 26 is for the 3rd reaction tower 28 carries available for reaction air；
In the present embodiment, catalyst stored in catalyst carrier 2 is homogeneous catalyst, and the homogeneous catalyst is sulfuric acid
Iron, ferric nitrate, copper sulphate, copper nitrate, manganese sulfate, manganese nitrate, cobaltous sulfate, cobalt nitrate, zinc sulfate, zinc nitrate, nickel sulfate, nitric acid
One or more in nickel, at can be preferably to high concentration highly salt containing organic waste water after above-mentioned homogeneous catalyst
Reason, high treating effect；
In the present embodiment, heterogeneous catalyst is filled with the 3rd reaction tower 28, described heterogeneous catalyst is noble-metal-supported
Type catalyst, its carrier be activated carbon, titanium dioxide, zirconium dioxide, alundum (Al2O3), SiO 2 molecular sieve in one kind or
Multiple combination, its active component is one or more in ruthenium, rhodium, palladium, silver, platinum, cerium, lanthanum, neodymium, using above-mentioned heterogeneous catalyst
After preferably high concentration highly salt containing organic waste water can be processed, high treating effect；
The operation principle of wastewater treatment equipment of the present invention is as follows：
The high concentration highly salt containing organic waste water that the first membrane pump 4 will be stored in waste water storage tank 1 is first passed through to be passed through through the first pipeline 5
Pipe-line mixer 6, while the homogeneous catalyst stored in catalyst carrier 2 is also passed into pipe-line mixer through the second pipeline 7
6, while making air compressor machine 3 that reaction air is also passed into pipe-line mixer 6 by the 3rd pipeline 8, now high concentration saliferous high has
Machine waste water, homogeneous catalyst and air three enter the after mixing in the pipe-line mixer 6 from the charging aperture of First Heat Exchanger 9
One heat exchanger 9, then from the discharging opening of First Heat Exchanger 9 into the first reaction tower 10 in carry out sufficient Characteristic of Homogenous Catalytic Wet Air Oxidation
Reaction, the first road treatment water that the first reaction tower 10 will can be formed after reaction enters the 4th pipe from the top exit of the first reaction tower 10
Road 12, then enter the charging aperture of the second heat exchanger 11 from the 4th pipeline 12, now reaction can be passed through the tenth by air compressor machine 3 with air
Five pipelines 36 are also passed into the charging aperture of the second heat exchanger 11, and the first reaction tower 10 first road treatment water out can be with air second
Mix in heat exchanger 11 and sufficiently exchanged heat with the water in the second heat exchanger 11, the water in the second heat exchanger 11 is through heat exchange
After can become steam and generated electricity for turbine generators, and treatment water in two roads is then entered and carried out in the second reaction tower 13 after heat exchange cooling
Second Characteristic of Homogenous Catalytic Wet Air Oxidation reacts, and two roads that the second reaction tower 13 will can be formed after reaction process water from the second reaction tower
13 top exit enters the 5th pipeline 15, then enters First Heat Exchanger 9, Ran Houzai from the heat exchange water inlet of First Heat Exchanger 9
Enter the 6th pipeline 16 from the heat exchange water out of First Heat Exchanger 9, the discharge of the second reaction tower 13 two roads treatment water by the
During one heat exchanger 9, two roads treatment water waste heat can by the high concentration highly salt containing organic waste water by First Heat Exchanger 9,
Homogeneous catalyst and air three absorb, so as to high concentration highly salt containing organic waste water, the homogeneous catalysis by First Heat Exchanger 9
Agent and air three mixture carry out heat temperature raising, and itself then gradually cools after heat exchange；
Now gas-liquid can be carried out in the 6th pipeline 16 into the first gas-liquid separator 17 by the roads of the Hou bis- treatment water that cools
Separate, the first gas-liquid separator 17 two roads is processed the gas phase generated after water gas-liquid separation and enters the first tail gas through the 7th pipeline 18
Absorption tower 19, is carried out being discharged after treatment is up to standard through the first tail gas absorber 19, and two roads are processed water by the first gas-liquid separator 17
The liquid phase generated after gas-liquid separation can enter the first dashpot 21 through the 8th pipeline 20, then by the second membrane pump 22 through the 9th pipeline
23 squeeze into MVR evaporators 24 is processed, and the remaining mother liquor of steaming and condensed water can be formed after the treatment of MVR evaporators 24, wherein steaming remaining female
Liquid can be used for reuse and prepare homogeneous catalyst, and condensed water then squeezes into the 3rd heat exchanger by the 3rd membrane pump 25 through the tenth pipeline 26
Reaction air be also passed into the charging of the 3rd heat exchanger 27 by the 16th pipeline 37 for 27 charging aperture, the now meeting of air compressor machine 3
Mouthful, condensed water is passed through the 3rd reaction tower after mixing in the 3rd heat exchanger 27 with air from the discharging opening of the 3rd heat exchanger 27
28, and sufficient heterogeneous catalysis humidifying oxidation reaction is carried out together with the heterogeneous catalyst in the 3rd reaction tower 28, the 3rd reaction
The three roads treatment water that tower 28 will can be formed after reaction enters the 11st pipeline 29, then changing from the 3rd heat exchanger 27 from top exit
Hot water inlet enters the 3rd heat exchanger 27, and then the heat exchange water out again from the 3rd heat exchanger 27 enters the 12nd pipeline 30,
During three roads formed after the CWO reaction of the discharge of the 3rd reaction tower 28 process water by the 3rd heat exchanger 27,
The waste heat of three road treatment water can be absorbed by the condensed water of the 3rd heat exchanger 27 with air, so as to by the 3rd heat exchange
Condensed water and air in device 27 carry out heat temperature raising, and itself then gradually cools after heat exchange；At cooling Hou tri- roads
Reason water can enter the 12nd pipeline 30 from the heat exchange of the 3rd heat exchanger 27 mouth, then enter the second gas-liquid separation from the 12nd pipeline 30
Device 31, the second gas-liquid separator 31 generates gas phase and liquid phase, the gas phase meeting for being generated after three roads treatment water is carried out into gas-liquid separation
Entered through the 13rd pipeline 32 after second tail gas absorber 33 carries out treatment up to standard and discharged, and the liquid phase for being generated can be through the 14th
Pipeline 34 enters the second dashpot 21, then is directly discharged into extraneous from the second dashpot 21 or enters biochemical system treatment, by upper
Operation is stated, that is, completes the treatment to high concentration highly salt containing organic waste water.
The advantage of wastewater treatment equipment of the present invention is：（1）Processing cost is low, high treating effect, floor space are small and automatic
Change degree is high；（2）Waste water need not be diluted, it is possible to directly process COD contents more than 100,000 mg/L and the waste water of high salinity；
（3）In the absence of the secondary pollution to environment in wastewater treatment process；（4）Waste heat is reclaimed by heat exchanger, and will heat exchange
The steam that device is produced generates electricity for turbine generators, has reached the purpose that energy regenerating is utilized.
A kind of method of wastewater treatment, comprises the following steps：
（1）A kind of organic intermediate production waste water is processed, the waste water mainly contains 1, the composition such as hydroresorcinol, sodium chloride, COD
It is 125360 mg/L, pH=3.5, salinity is 12.5%；Heated up again after first homogeneous catalyst is mixed with waste water and be passed through the first reaction
Tower, is mixed with the waste water and the first reaction tower of homogeneous catalyst by the reaction of air compressor machine offer with air together in the first reaction tower
Inside carry out first time Characteristic of Homogenous Catalytic Wet Air Oxidation reaction, first road treatment water of the generation comprising homogeneous catalyst；Wherein homogeneous catalysis
The reaction condition of wet oxidation reaction is：Reaction temperature is（250~300）DEG C, reaction pressure is（4.5~9）MPa, liquid hourly space velocity (LHSV)
For（0.5~3） h-1, the dosage of wherein homogeneous catalyst is that every liter of waste water is added（50~500）mg；
（2）Then by step（1）The second reaction tower is passed through after the first road treatment water cooling of generation, then Shi Chu roads treatment water and the
The reaction provided by air compressor machine in two reaction towers carries out second homogeneous catalysis wet type oxygen with air in the second reaction tower together
Change reaction, two roads treatment water of the generation comprising homogeneous catalyst, the reaction condition of wherein Characteristic of Homogenous Catalytic Wet Air Oxidation reaction is：Instead
The temperature is answered to be（220~290）DEG C, reaction pressure is（2.5~8）MPa, liquid hourly space velocity (LHSV) is（0.5~3） h-1, wherein homogeneous catalyst
Dosage be that every liter of waste water is added（50~500）mg；
（3）Then by step（2）Being passed through the first gas-liquid separator after the two roads treatment water cooling of generation carries out gas-liquid separation, generates
Gas phase and the liquid phase containing homogeneous catalyst；
（4）Then by step（3）The liquid phase of generation is passed through MVR evaporators and is evaporated, and generates colourless crystallization salt, condensed water and contains
The evaporation conditionses for having mother liquor more than the steaming of homogeneous catalyst, wherein MVR evaporators are：Evaporating temperature is（50~100）DEG C, steam remaining female
Liquid measure is controlled in step（3）The amount of liquid phase of generation（1~10）%；
（5）Then by step（4）The condensed water of generation is passed through the 3rd reaction tower, multiphase in condensed water and the 3rd reaction tower after heating up
Catalyst and by air compressor machine provide reaction carry out heterogeneous catalysis wet oxidation reaction in the 3rd reaction tower together with air,
Three roads treatment water is generated, the reaction condition of wherein heterogeneous catalysis wet oxidation reaction is：Reaction temperature is（180~280）DEG C, instead
The pressure is answered to be（2.0~7.5）MPa, liquid hourly space velocity (LHSV) is（0.5~3） h-1；
（6）Then by step（5）Being passed through the second gas-liquid separator after the three roads treatment water cooling of generation carries out gas-liquid separation, generates
Gas phase and meet the liquid phase of discharge standard.
Described homogeneous catalyst is ferric sulfate, ferric nitrate, copper sulphate, copper nitrate, manganese sulfate, manganese nitrate, cobaltous sulfate, nitre
One or more in sour cobalt, zinc sulfate, zinc nitrate, nickel sulfate, nickel nitrate.
Described heterogeneous catalyst is noble metal carrier catalyst, and its carrier is activated carbon, titanium dioxide, titanium dioxide
One or more in zirconium, alundum (Al2O3), silica and molecular sieve combination, its active component be ruthenium, rhodium, palladium, silver, platinum,
One or more in cerium, lanthanum, neodymium.
Following table is raw wastewater by after the reaction of Characteristic of Homogenous Catalytic Wet Air Oxidation twice and anti-by heterogeneous catalysis wet oxidation
Should after COD, COD clearance, salt content and pH value in the treatment water that obtains, and it can be seen that this wastewater treatment side from table
The high treating effect of method.
The advantage of method of wastewater treatment of the present invention is：Good treatment efficiency, COD clearances are high, and COD clearances are more than 95%, in waste water
In the absence of the secondary pollution to environment in processing procedure, and waste water need not be diluted, it is possible to directly process COD contents more than 10
The waste water of ten thousand mg/L and high salinity, especially has more advantage to the treatment volatile waste water of organic principle, and MVR steams remaining mother liquor reuse
Homogeneous catalyst is prepared not only to have solved the problems, such as concentrate and reached the purpose that recycles, and it is colourless cleaning to separate out salt
Salt, recyclable recycling.
Claims (10)
1. energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit, it is characterised in that：Waste water storage including being used to store waste water
Groove, it is used to store the catalyst carrier and air compressor machine of catalyst, the delivery port of the waste water storage tank and going out for catalyst carrier
Material mouth is communicated with the charging aperture of First Heat Exchanger simultaneously, and the discharging opening of First Heat Exchanger is communicated with the import of the first reaction tower, the
The outlet of one reaction tower is communicated with the charging aperture of the second heat exchanger, the import phase of the discharging opening of the second heat exchanger and the second reaction tower
It is logical, the heat exchange water out connection turbine generators of second heat exchanger, the outlet of second reaction tower is through First Heat Exchanger
Import with the first gas-liquid separator is connected, the import phase of the gaseous phase outlet of the first gas-liquid separator and the first tail gas absorber
Connection, the liquid-phase outlet of the first gas-liquid separator is connected with the charging aperture of MVR evaporators, the condensation-water drain of MVR evaporators
Charging aperture with the 3rd heat exchanger is connected, and the discharging opening of the 3rd heat exchanger is connected with the import of the 3rd reaction tower, and the 3rd is anti-
Answer the outlet of tower to be connected with the import of the second gas-liquid separator through the 3rd heat exchanger, the gaseous phase outlet of the second gas-liquid separator with
The import of the second tail gas absorber is connected；The air compressor machine is simultaneously the first reaction tower by pipeline, the second reaction tower and the
Three reaction towers carry available for reaction air.
2. energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit according to claim 1, it is characterised in that：Second is anti-
The outlet of tower is answered to be connected with the shell of First Heat Exchanger, with thermal material adverse current by First Heat Exchanger, first exchanges heat cold material
The shell outlet of device is connected with the import of the first gas-liquid separator.
3. energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit according to claim 1, it is characterised in that：3rd is anti-
The outlet of tower is answered to be connected with the shell of the 3rd heat exchanger, cold material is with thermal material adverse current by the 3rd heat exchanger, the 3rd heat exchange
The shell outlet of device is connected with the import of the second gas-liquid separator.
4. energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit according to claim 1, it is characterised in that：First gas
The liquid-phase outlet of liquid/gas separator is connected with the charging aperture of the first dashpot, discharging opening and the MVR evaporators of the first dashpot
Charging aperture is connected.
5. energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit according to claim 1, it is characterised in that：MVR steams
Mother liquor reflux is sent out more than the steaming of device to catalyst carrier.
6. a kind of method of wastewater treatment, it is characterised in that：Using the device as described in any one of Claims 1 to 5, and including such as
Lower step：
（1）Heated up again after first homogeneous catalyst is mixed with waste water and be passed through the first reaction tower, be mixed with homogeneous catalyst waste water and
The reaction provided by air compressor machine in first reaction tower carries out first time homogeneous catalysis wet type in the first reaction tower together with air
Oxidation reaction, first road treatment water of the generation comprising homogeneous catalyst；
（2）Then by step（1）The second reaction tower is passed through after the first road treatment water cooling of generation, then Shi Chu roads treatment water and the
The reaction provided by air compressor machine in two reaction towers carries out second homogeneous catalysis wet type oxygen with air in the second reaction tower together
Change reaction, two roads treatment water of the generation comprising homogeneous catalyst；
（3）Then by step（2）Being passed through the first gas-liquid separator after the two roads treatment water cooling of generation carries out gas-liquid separation, generates
Gas phase and the liquid phase containing homogeneous catalyst；
（4）Then by step（3）The liquid phase of generation is passed through MVR evaporators and is evaporated, and generates colourless crystallization salt, condensed water and contains
There is mother liquor more than the steaming of homogeneous catalyst；
（5）Then by step（4）The condensed water of generation is passed through the 3rd reaction tower, multiphase in condensed water and the 3rd reaction tower after heating up
Catalyst and by air compressor machine provide reaction carry out heterogeneous catalysis wet oxidation reaction in the 3rd reaction tower together with air,
Generate three roads treatment water；
（6）Then by step（5）Being passed through the second gas-liquid separator after the three roads treatment water cooling of generation carries out gas-liquid separation, generates
Gas phase and meet the liquid phase of discharge standard；
Described homogeneous catalyst is ferric sulfate, ferric nitrate, copper sulphate, copper nitrate, manganese sulfate, manganese nitrate, cobaltous sulfate, nitric acid
One or more in cobalt, zinc sulfate, zinc nitrate, nickel sulfate, nickel nitrate；
Described heterogeneous catalyst is noble metal carrier catalyst, and its carrier is activated carbon, titanium dioxide, zirconium dioxide, three
One or more in Al 2 O, silica and molecular sieve combination, its active component be ruthenium, rhodium, palladium, silver, platinum, cerium, lanthanum,
One or more in neodymium.
7. a kind of method of wastewater treatment according to claim 6, it is characterised in that：Step（1）Middle homogeneous catalysis wet type oxygen
Changing the reaction condition for reacting is：Reaction temperature is（250~300）DEG C, reaction pressure is（4.5~9）MPa, liquid hourly space velocity (LHSV) is（0.5
~3） h-1, the dosage of wherein homogeneous catalyst is that every liter of waste water is added（50~500）mg.
8. a kind of method of wastewater treatment according to claim 6, it is characterised in that：Step（2）Middle homogeneous catalysis wet type oxygen
Changing the reaction condition for reacting is：Reaction temperature is（220~290）DEG C, reaction pressure is（2.5~8）MPa, liquid hourly space velocity (LHSV) is（0.5
~3） h-1, the dosage of wherein homogeneous catalyst is that every liter of waste water is added（50~500）mg.
9. a kind of method of wastewater treatment according to claim 6, it is characterised in that：Step（4）The evaporation of middle MVR evaporators
Condition is：Evaporating temperature is（50~100）DEG C, remaining mother liquor amount control is steamed in step（3）The amount of liquid phase of generation（1~10）%.
10. a kind of method of wastewater treatment according to claim 6, it is characterised in that：Step（5）Middle heterogeneous catalysis wet type oxygen
Changing the reaction condition for reacting is：Reaction temperature is（180~280）DEG C, reaction pressure is（2.0~7.5）MPa, liquid hourly space velocity (LHSV) is
（0.5~3） h-1。
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| CN108383231A (en) * | 2018-03-09 | 2018-08-10 | 涂学炎 | A method of based on MVR system two-phase catalytic treatments high concentrated organic wastewater with high salt |
| CN108383231B (en) * | 2018-03-09 | 2021-01-12 | 涂学炎 | Method for double-phase catalytic treatment of high-salt high-concentration organic wastewater based on MVR system |
| CN109293116A (en) * | 2018-11-07 | 2019-02-01 | 苏州工业园区承叶环境科技有限公司 | A kind for the treatment of process of high concentration cymoxanil waste water |
| CN109179791A (en) * | 2018-11-16 | 2019-01-11 | 佛山科学技术学院 | A kind of catalytic wet oxidation processing equipment of the industrial wastewater with multistage filtering |
| CN112694163A (en) * | 2019-10-23 | 2021-04-23 | 中国石油化工股份有限公司 | Method for quenching waste water of catalytic wet-type acrylonitrile oxidation device |
| CN110921806A (en) * | 2019-12-12 | 2020-03-27 | 山东沾化金嘉利化工科技有限公司 | Oxidation treatment method of calcium chloride-containing high-salinity wastewater |
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