CN107794214A - The Waste Water Treatment of removal organic polluter and sulphur is removed simultaneously - Google Patents
The Waste Water Treatment of removal organic polluter and sulphur is removed simultaneously Download PDFInfo
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- CN107794214A CN107794214A CN201610802987.8A CN201610802987A CN107794214A CN 107794214 A CN107794214 A CN 107794214A CN 201610802987 A CN201610802987 A CN 201610802987A CN 107794214 A CN107794214 A CN 107794214A
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- sulphur
- waste water
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- bioreactor
- separator
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 239000005864 Sulphur Substances 0.000 title claims abstract description 57
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 32
- 239000010802 sludge Substances 0.000 claims abstract description 73
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 70
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 65
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 claims abstract description 38
- 229940006486 zinc cation Drugs 0.000 claims abstract description 38
- 238000004140 cleaning Methods 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 239000000203 mixture Substances 0.000 claims abstract description 13
- 238000005276 aerator Methods 0.000 claims abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims description 62
- 239000002351 wastewater Substances 0.000 claims description 53
- 238000007872 degassing Methods 0.000 claims description 45
- 238000001556 precipitation Methods 0.000 claims description 42
- 238000000926 separation method Methods 0.000 claims description 11
- 230000002829 reductive effect Effects 0.000 claims description 10
- 239000003513 alkali Substances 0.000 claims description 7
- 239000013530 defoamer Substances 0.000 claims description 7
- 239000002244 precipitate Substances 0.000 claims description 4
- 230000001376 precipitating effect Effects 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 239000011573 trace mineral Substances 0.000 claims description 3
- 235000013619 trace mineral Nutrition 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 53
- 238000000034 method Methods 0.000 description 24
- 229910052739 hydrogen Inorganic materials 0.000 description 23
- 239000001257 hydrogen Substances 0.000 description 23
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 21
- 230000000694 effects Effects 0.000 description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 19
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 19
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 18
- 230000008569 process Effects 0.000 description 16
- 241000894006 Bacteria Species 0.000 description 15
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 13
- 238000000855 fermentation Methods 0.000 description 12
- 239000012071 phase Substances 0.000 description 11
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 9
- 231100000419 toxicity Toxicity 0.000 description 9
- 230000001988 toxicity Effects 0.000 description 9
- 239000000463 material Substances 0.000 description 8
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 7
- 239000001569 carbon dioxide Substances 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 230000008859 change Effects 0.000 description 7
- 239000011159 matrix material Substances 0.000 description 7
- 244000005700 microbiome Species 0.000 description 7
- 239000000047 product Substances 0.000 description 7
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 238000007667 floating Methods 0.000 description 6
- 230000007062 hydrolysis Effects 0.000 description 6
- 238000006460 hydrolysis reaction Methods 0.000 description 6
- 230000000670 limiting effect Effects 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 231100000331 toxic Toxicity 0.000 description 6
- 230000002588 toxic effect Effects 0.000 description 6
- 210000004027 cell Anatomy 0.000 description 5
- 238000009833 condensation Methods 0.000 description 5
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- 238000006477 desulfuration reaction Methods 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 5
- 150000003464 sulfur compounds Chemical class 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 230000029087 digestion Effects 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000020477 pH reduction Effects 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 3
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 3
- 229920002472 Starch Polymers 0.000 description 3
- 235000011054 acetic acid Nutrition 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
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- 229930195729 fatty acid Natural products 0.000 description 3
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- 150000004665 fatty acids Chemical class 0.000 description 3
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- 235000019698 starch Nutrition 0.000 description 3
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- 241001148471 unidentified anaerobic bacterium Species 0.000 description 3
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 description 2
- 241000589516 Pseudomonas Species 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
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- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 2
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- 102000004169 proteins and genes Human genes 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
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- FERIUCNNQQJTOY-UHFFFAOYSA-M Butyrate Chemical compound CCCC([O-])=O FERIUCNNQQJTOY-UHFFFAOYSA-M 0.000 description 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 244000025254 Cannabis sativa Species 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
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- BDAGIHXWWSANSR-UHFFFAOYSA-N Formic acid Chemical compound OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 241000605118 Thiobacillus Species 0.000 description 1
- 208000036142 Viral infection Diseases 0.000 description 1
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- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 229910002056 binary alloy Inorganic materials 0.000 description 1
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- 230000000593 degrading effect Effects 0.000 description 1
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- 239000005446 dissolved organic matter Substances 0.000 description 1
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- 239000008103 glucose Substances 0.000 description 1
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- 239000010440 gypsum Substances 0.000 description 1
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- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 1
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- 150000004763 sulfides Chemical class 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
- C02F3/341—Consortia of bacteria
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
- C02F3/345—Biological treatment of water, waste water, or sewage characterised by the microorganisms used for biological oxidation or reduction of sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
-
- 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
- C02F2101/101—Sulfur compounds
-
- 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
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
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- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
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- Wood Science & Technology (AREA)
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- Biotechnology (AREA)
- Genetics & Genomics (AREA)
- General Engineering & Computer Science (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Sustainable Development (AREA)
- Biomedical Technology (AREA)
- Molecular Biology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
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Abstract
The invention discloses a kind of while remove the Waste Water Treatment of removal organic polluter and sulphur, including：Anaerobic reactor；Zinc cation tower, zinc cation tower are connected with the exhaust outlet of anaerobic reactor；Methane voltage-stabilizing cabinet natural pond；Bioreactor, is provided with aerator in bioreactor, bioreactor is connected with zinc cation tower, for into zinc cation tower supply cleaning solution to wash the gas being supplied to out of anaerobic reactor in zinc cation tower；Sulphur settling vessel, sulphur settling vessel have inlet, liquid outlet and elemental sulfur sludge outlet, and inlet and liquid outlet are connected with bioreactor, are supplied to from a part for the cleaning solution of bioreactor discharge in sulphur settling vessel to isolate elemental sulfur from cleaning solution；And separator for mud and water, separator for mud and water are connected with anaerobic reactor, for being separated to the mud mixture of the delivery port discharge from anaerobic reactor.
Description
Technical field
The present invention relates to technical field of waste water processing, in particular it relates to a kind of organic dirt that can be removed in waste water simultaneously
Contaminate the Waste Water Treatment of thing and sulphur.
Background technology
For the waste water containing high concentration COD and high sulfate radical simultaneously, if sulfate radical is reduced into sulfurous acid sulfate radical
Or exceed the inhibition concentration of methanogen after free curing hydrogen, inhibitory action will be produced to methanogen, methane phase speed reduces
Or stop.If suppressing the time reaches certain degree, the activity of methanogen can not be recovered.
In addition, total sulfur compound equally exists toxicity to sulfate reducing bacteria.If the total sulfur compound concentration in waste water exceedes
Certain threshold value, the activity of sulfate reducing bacteria can be also suppressed, and sulfate reduction can not also continue, therefore, it is necessary to
Remove the sulfate radical and organic pollution in waste water.
In correlation technique the sulfate radical and organic pollution in waste water are removed using following methods：A kind of method is to waste water
In sulfate radical pre-processed.For example, removing part of sulfuric acid root using the method for adding calcium ion formation gypsum, it will enter and detest
The sulfate concentration of oxygen processing system is reduced to below safe concentration.But this method pharmaceutical quantities that need to add are big and produce
Secondary pollution.Another method is to carry out stripping to the anaerobic effluent after Anaerobic Treatment, after the hydrogen sulfide stripping of formation is fallen, then
Anaerobic effluent after stripping is returned into anaerobic reactor water inlet, dilutes the total sulfur compound concentration in anaerobic reactor.But such as
Fruit sulfate concentration is high, and the volume of stripping reactor is big, the high energy consumption of stripping, and stripping uses inert gas, and consumption is big,
Cost is high.
The content of the invention
It is contemplated that at least solves one of technical problem in correlation technique to a certain extent.Therefore, the present invention
It is proposed a kind of Waste Water Treatment of the sulfate radical that can be removed simultaneously in waste water and organic pollution on one side.
The Waste Water Treatment of removal organic polluter and sulphur is removed while according to embodiments of the present invention, including：Anaerobic reaction
Device, the anaerobic reactor include anaerobic reaction room, stripping tube and air supply pipe, and the anaerobic reaction room has waste water inlet, gone out
The mouth of a river and exhaust outlet, the stripping tube are located in the anaerobic reaction room, and the upper end of the stripping tube has gas outlet and described
The lower end of stripping tube has air inlet, and the air supply pipe is connected with the air inlet of the stripping tube, for into the stripping tube
Supply the gas for air lift；Zinc cation tower, the zinc cation tower are connected with the exhaust outlet of the anaerobic reactor, are used for
The gas discharged from the anaerobic reactor is washed；Methane voltage-stabilizing cabinet, the methane voltage-stabilizing cabinet and the zinc cation
Tower is connected with the air inlet of the stripping tube, the biogas discharged for voltage stabilizing from the zinc cation tower and supplies a part of biogas
It is given in the stripping tube；Bioreactor, is provided with aerator in the bioreactor, the bioreactor with it is described
Zinc cation tower is connected, and is supplied to for supplying cleaning solution into the zinc cation tower with washing out of described anaerobic reactor
Gas in the zinc cation tower, the cleaning solution after washing gas are returned in the bioreactor；Sulphur settling vessel, it is described
Sulphur settling vessel has inlet, liquid outlet and elemental sulfur sludge outlet, and the inlet and the liquid outlet and the biology are instead
Answer device to be connected, be supplied to from a part for the cleaning solution of bioreactor discharge in the sulphur settling vessel with from cleaning solution
Isolate elemental sulfur；And separator for mud and water, the separator for mud and water are connected with the anaerobic reactor, for from the anaerobism
The mud mixture of the delivery port discharge of reactor is separated.
The Waste Water Treatment of removal organic polluter and sulphur is removed while according to embodiments of the present invention, by anaerobic reactor with
The biological desulphurization treatment apparatus that desulfurization process can be carried out is combined together, by reasonably designing, controlling in stripping biogas
The amount of hydrogen sulfide content and stripping biogas, the concentration of hydrogen sulfide in final waste water and biogas are up to a stable balance,
Enable removing COD in device and the continual and steady progress of desulphurization reaction, serve while remove removal organic polluter and sulfuric acid
The effect of root.
The Waste Water Treatment of removal organic polluter and sulphur is removed while according to embodiments of the present invention, can also be had as follows
Additional technical characteristic：
According to one embodiment of present invention, Waste Water Treatment that is described while removing removal organic polluter and sulphur also includes
Sinker, the sinker are connected between the anaerobic reactor and the separator for mud and water, for anti-from the anaerobism
Answer device to be supplied to the mud mixture of the separator for mud and water and carry out energy dissipating.
According to one embodiment of present invention, the sinker has to go out with what the exhaust outlet of the anaerobic reactor was connected
Gas port.
According to one embodiment of present invention, the sludge outlet of the separator for mud and water is connected with the anaerobic reactor,
It is supplied to from a part of sludge of separator for mud and water discharge in the anaerobic reactor, the anaerobic reactor also has surplus
Remaining sludge outlet.
According to one embodiment of present invention, Waste Water Treatment that is described while removing removal organic polluter and sulphur also includes
First Heat Exchanger, the First Heat Exchanger are used for that will be supplied to giving up in the anaerobic reactor by the waste water inlet
Water carries out heat exchange.
According to one embodiment of present invention, Waste Water Treatment that is described while removing removal organic polluter and sulphur also includes
Second heat exchanger, second heat exchanger are used to wash with being supplied to a part for the zinc cation tower from the bioreactor
Wash liquid and carry out heat exchange, the cleaning solution after heat exchange is returned in the bioreactor, and the bioreactor also has alkali
Liquid and trace element add mouth, and the defoamer for adding defoamer adds mouth.
According to one embodiment of present invention, a part of sludge of the elemental sulfur sludge outlet discharge of the sulphur settling vessel returns
Return in the bioreactor.
According to one embodiment of present invention, the anaerobic reactor also includes precipitation separator, the precipitation separator
It is located in the anaerobic reaction room and above the stripping tube, the precipitation separator has what is be connected with the delivery port
Separator delivery port.
According to one embodiment of present invention, the precipitation separator includes：Casing, the casing are interior heavy formed with degassing
Shallow lake chamber, the bottom of the degassing precipitation chamber have a sludge outlet, the cross-sectional area of the bottom of the degassing precipitation chamber along on to
Under direction be gradually reduced；Dividing plate, the dividing plate are located at the top of the degassing precipitation chamber, and the dividing plate precipitates the degassing
The top of chamber is separated into degassing district and settling zone, the bottom of the degassing district connected with the bottom of the settling zone so as to waste water from
The anaerobic reaction room overflows in the degassing district and then flowed to from the bottom of the degassing district in the settling zone；Precipitation is oblique
Plate, the precipitation inclined plate are located in the settling zone；Downflow weir, the downflow weir is located in the settling zone and the downflow weir
Form the overflow launder with the separator delivery port.
According to one embodiment of present invention, the upper edge that the box portion of the degassing district is limited with the dividing plate is less than
The upper edge of the dividing plate and the upper edge that the box portion of the settling zone is limited with the dividing plate, the casing are rectangular
Body, the lower end of the first longitudinal side wall of the bottom of the casing are extended downward beyond under the second longitudinal side wall of the bottom of the casing
End, and the lower end of first longitudinal side wall is overlapping in the vertical direction with the lower end of second longitudinal side wall.
Brief description of the drawings
The anaerobic reaction of the Waste Water Treatment of removal organic polluter and sulphur is removed while Fig. 1 is according to embodiments of the present invention
The structural representation of device.
Fig. 2 removes the Waste Water Treatment of removal organic polluter and sulphur while being according to an alternative embodiment of the invention
The structural representation of anaerobic reactor.
Fig. 3 removes the Waste Water Treatment of removal organic polluter and sulphur while being according to an alternative embodiment of the invention
The structural representation of the precipitation separator of anaerobic reactor.
The structural representation of the Waste Water Treatment of removal organic polluter and sulphur is gone while Fig. 4 is according to embodiments of the present invention
Figure.
Reference：
Anaerobic reactor 10,
Anaerobic fermentation tank body 100, anaerobic reaction room 110, waste water inlet 111, delivery port 112, exhaust outlet 113, substitute
Mouth 114,
Stripping tube 200, straight length 210, air inlet 211, segmental arc 220, gas outlet 221,
Air supply pipe 300,
Precipitate separator 400, casing 410, degassing precipitation chamber 411, sludge outlet 412, separator delivery port 413, first
Longitudinal side wall 414, the second longitudinal side wall 415, dividing plate 420, degassing district 421, settling zone 422, precipitation inclined plate 430, downflow weir 440, overflow
Chute 441,
Sinker 61, gas outlet 611,
Mud return line 600,
Sludge discharge pipe 700,
Zinc cation tower 20, methane voltage-stabilizing cabinet 30, bioreactor 40, moisturizing unit 401, sulphur settling vessel 50, muddy water point
From device 60, condensation water tank 70, First Heat Exchanger 80, the second heat exchanger 90.
Embodiment
Embodiments of the invention are described below in detail, the example of the embodiment is shown in the drawings.Below with reference to
The embodiment of accompanying drawing description is exemplary, it is intended to for explaining the present invention, and is not considered as limiting the invention.
Only these materials can be just converted after sludge has adapted to (being difficult to what is be degraded) matrix of complexity.Adapt to matrix
The time microorganism special with required matrix degradation growth it is closely related.
Anaerobic digestion process can be divided into four relatively independent but inseparable steps：Hydrolysis stage, souring stage, production
Hydrogen produces acetic acid stage and methane phase stage.
Acidification bacteria completes the first two steps of anaerobic digestion process, that is, hydrolyzes and be acidified.They will be poly- by ectoenzyme
Compound such as protein, fat and carbohydrate inversion is can enter the small-molecule substance of cell interior, and portion aoxidizes in the cell
Degrade and form carbon dioxide (CO2), hydrogen (H2) and primary product-volatile fatty acid (VFA).
Above-mentioned product is converted into acetate, hydrogen and dioxy by second group of microorganism, hydrogen-producing acetogens in acidization
Change carbon.
3rd group of microorganism is methanogen, and acetate or hydrogen and carbon dioxide conversion are methane by they.
Other matrix such as formates (HCOOH) that there may be and utilized by methanogen, methanol (CH3OH), an oxygen
Change carbon (CO) and methylamine etc., inferior critical role is in anaerobic wastewater treatment plants.
Hydrolysis may be defined as complexity matrix not soluble in water be converted into by the ectoenzyme that Institute of Micro-biology secretes it is smaller
Water-soluble matrix process.The process that organic matter is hydrolyzed is a relatively slow process, and its reaction rate is with being permitted
Multi-parameter is relevant, and the compatibility of wherein pH value (Optimal pH=6), biological concentration and matrix is mostly important.Generally speaking particle is got over
Big affinity is lower.
Although most biopolymer is bio-degradable, material fibrils element (grass, the timber of height lignifying
Deng) extremely difficult hydrolysis, initially with the activity of the reaction of the enzyme of cellulose depending on selective microbe.Half different from cellulose is fine
Dimension element can be degraded by many Institute of Micro-biology；The main component of the third cellulosic material-lignin is under anaerobic can not
It is degraded.
The conversion of fat is a relatively slow process, due to contain substantial amounts of fatty material in waste water, hydrolyze just into
For the rate limit of whole conversion process.At 20 DEG C, the conversion ratio of fat is almost nil.Other are slow and complicated process relates to
And conversion of many different types of anaerobes to protein.
Starch material is equally difficult to be hydrolyzed., must before waste water enters anaerobic reactor when handling wastewater of starch factory
The particulate matter in waste water must be removed first or is allowed to appropriate hydrolysis, and otherwise starch material can accumulate in reactor, acidifying
And the pH extremely harmful to reactor is caused to decline.By controlling enough hydraulic detention times and control pH value of waste water left 6
The right side can obtain appropriate degree of hydrolysis.
In acidization, dissolved organic matter is converted mainly into volatile fatty acid.In the fat that this step is formed
The type of fat acid depends primarily on environmental factor, initial substance and active microorganism population.
Transforming glucose (enters in different reactors respectively in souring stage and methane phase stage in acidification reactor
First phase of capable binary system) generation butyric acid, acetic acid, propionic acid, lactic acid, ethanol, the mixture of hydrogen and carbon dioxide, then have
After machine aliphatic acid and carbon dioxide mixture produce, turn into one of final product if amino acid is converted ammonification.
Acidification bacteria has very wide pH tolerances, and with the continuous formation of acidic materials, final pH can be down to 4 or so.
Methanogen has its optimal pH accommodation：PH6.5~7.5.Once disappearing for acidizing product hydrogen can be caused beyond the pH scopes
Consumption slows down.
The product of acid-producing bacteria is converted into acetate by hydrogen-producing acetogens and is finally converted into hydrogen and titanium dioxide by methanogen
Carbon.Ethanol, butyrate, propionate do not produce energy (free energy during being converted into acetate and hydrogen in normal conditions
Change turns to negative value and indicates energy production).The acetate only in liquid in the presence of methanogen and sulfate reducing bacteria
Concentration, it is often more important that then hydrogen-producing acetogens just carry out these reactions when the hydrogen dividing potential drop in liquid is sufficiently low.
The transfer time of hydrogen only within part second, such as due to the injustice between acidification and methanogenesis
The accumulation of hydrogen can hastily suppress the conversion of volatile fatty acid caused by weighing apparatus.The conversion of propionate can be affected at first,
Because the degraded of propionate is least easily carried out for thermodynamically.
This point is it is clear that either hydrolysis is still acidified and still hydrogenesis and acetogenesis stage nonevent COD is notable
Reduce, be in fact only the conversion reaction for being converted into another COD forms from a kind of form there occurs COD, final COD is gone
Except occurring in the methane phase stage, COD is converted into methane and removed from water herein.
The strict anaerobic bacteria of methane phase Pseudomonas and compared with other most of anaerobic bacterias methanogen growth need it is lower
Oxidation-reduction potential (<- 330mV).
Methane phase Pseudomonas can be divided into two main populations：Acetic acid degrading bacteria and hydrogen utilize bacterium (thermophilic hydrogen bacterium).Another microspecies
Group can utilize acetate and can to produce methane using hydrogen and carbon dioxide.Some thermophilic producing hydrogen and methane bacterium can also convert formates
For methane.
In the complicated waste water of anaerobic digestion, acid-producing bacteria and acetogen synergy, the substrate second for reacting methane phase
The ratio that hydrochlorate and hydrogen are formed is fairly constant.The methane formed has 70~75% to be transformed remaining then by hydrogen by acetate
With carbon dioxide conversion.
The waste water of many industrial discharge containing sulfates and/or sulphite, during Anaerobic Treatment, sulfate (SO4 2-)
With sulphite (SO3 2-) it is reduced to hydrogen sulfide (H2S)。
Sulfate (the SO during Anaerobic Treatment4 2-) and/or sulphite (SO3 2-) reduction there are many shortcomings：Example
Such as Peculiar Smell, reduce COD transformation efficiency, water and Air Interface etching problem, reduce the quality of biogas, due to hydrogen sulfide
Toxicity make sludge activity reduce etc..
Sulfate is a compound for being relatively free of toxicity in itself.The product sulfur that sulfate reduces after the effect of anaerobic bacteria
Change hydrogen has toxicity to methanogen.And when the excessive concentration of sulfate, hyperosmosis will be to harmful microorganism.Therefore do not wish
Hope in waste water containing excessive sulfate.
Sulphite is virose compound.Anaerobic digestion process can in reduction system the toxic chemical total amount,
Because the hydrogen sulfide formed is largely discharged with biogas.
In general when sulfite concentration reaches 150~250ppm, 50% methanogenesis activity is suppressed (can be with
The species of substrate and it is different).But methanogen can gradually adapt to the toxicity of sulphite.After sludge adapts to its
Toxicity is smaller 70 times than original.
Usual reactor is continuously exposed to performance and non-hazardous of the sulphite to reactor, but fluctuates widely just and have
Harmfulness.Recommend to set a pre-acidified pond before anaerobic reactor is entered sometimes so that sulphite is anti-into anaerobism
Answer and reduced before device.
The toxicity of hydrogen sulfide is the considerable factor that must pay attention to.In the waste water containing sulfate, when in waste water
There are enough COD and residence time long enough, sulfate will be reduced to hydrogen sulfide.The toxicity of hydrogen sulfide mainly by its it is non-from
(the H of dissolving caused by the hydrogen sulfide of solution state2S), because it can permeating cell membranes, and HS-And S2-Do not possess this
Ability.
One-level dissociation equilibrium (the H at 30 degrees Celsius2S/HS-) equilibrium constant pKa be 6.9, it means that i.e. when pH is
H when 6.92S and HS-Quantity is equal.Anaerobic processes are also 6.9 or so progress in pH, and change small pH can be to reactor efficiency
Produce important influence.In the presence of the hydrogen sulfide for having the non-dissociation of 150mg/L, the production first of 70~75% methane productions is generally responsible for
The maximum specific methanogenic activity of alkane bacterium can decline 50%.
Influence of the pH changes to S balances is as follows：When pH rises, the H of non-dissociated dissolving is not dissociated2S toxic effects compared with
It is low, H in biogas2S concentration is relatively low, and sulfide concentration is higher in reactor water outlet；When the ph is lowered, it is understood that there may be non-dissociated molten
The H of solution2S toxic effects, H in biogas2S concentration is higher, and sulfide concentration is relatively low in reactor water outlet.
In the first situation, if it is expected that the water inlet containing sulfate can be problematic, COD can be used：SO4 2-(weight) compares
To estimate.Reactor is designed by a certain mud load rate (kgCOD/kgVSS/d), COD：SO4 2-It is higher, then hydrogen sulphide load
(H2S/kgVSS/d) lower, corresponding toxic effect is also lower.If this ratio is 10:1 or so then toxic action can neglect
Slightly, for the sludge tamed, this ratio even up to 5:1 and without obvious problem.
The pH of water inlet is improved in some cases to reducing H2S toxic effect can be helpful.As it was previously stated, in liquid phase not
The amount of the hydrogen sulfide (toxic forms) of dissociation can be reduced in pH compared with relative superiority or inferiority.
For the waste water containing high concentration COD and high sulfate radical simultaneously, if sulfate radical is reduced into sulfurous acid sulfate radical
Or exceed the inhibition concentration of methanogen after free curing hydrogen, inhibitory action, methane phase speed drop will be produced to methanogen
Low or stopping.If the time suppressed reaches certain degree, the activity of methanogen can not be recovered.
In addition, total sulfur compound equally exists toxicity to sulfate reducing bacteria.If the total sulfur compound concentration in waste water exceedes
Certain threshold values, the activity of sulfate reducing bacteria can be also suppressed, and sulfate reduction can not also continue, anaerobic reactor
In sulfate radical and organic pollution cannot effectively remove.
In view of above-mentioned technical problem, the present invention proposes a kind of sulfate radical and organic contamination that can be removed simultaneously in waste water
The Waste Water Treatment 1 of thing.
Gone while specifically describing according to embodiments of the present invention below in conjunction with the accompanying drawings at the waste water of removal organic polluter and sulphur
Reason system 1.
As shown in Figures 1 to 4, the Waste Water Treatment of removal organic polluter and sulphur is removed while according to embodiments of the present invention
1 includes anaerobic reactor 10, zinc cation tower 20, methane voltage-stabilizing cabinet 30, bioreactor 40, sulphur settling vessel 50 and mud-water separation
Device 60.
Specifically, anaerobic reactor 10 includes anaerobic fermentation tank body 100, stripping tube 200 and air supply pipe 300.Anaerobism is sent out
There is anaerobic reaction room 110 in fermentation tank body 100, anaerobic reaction room 110 has waste water inlet 111, delivery port 112 and exhaust outlet
113.The pipe of stripping tube 200 is located in anaerobic reaction room 110, and the upper end of stripping tube 200 has a gas outlet 221, and stripping tube 200
Lower end has air inlet 211.Air supply pipe 300 is connected with the air inlet 211 of stripping tube 200, is used for being supplied into stripping tube 200
In the gas of air lift.The gas for being used for air lift can be oxygen-depleted gas or inert gas, preferably biogas.
Zinc cation tower 20 is connected with the exhaust outlet 113 of anaerobic reactor 10, for discharging from anaerobic reactor 10
Gas is washed, and methane voltage-stabilizing cabinet 30 is connected with the air inlet 211 of zinc cation tower 20 and stripping tube 200, for voltage stabilizing from
Zinc cation tower 20 discharge biogas and a part of biogas is supplied in stripping tube 200.Aeration is provided with bioreactor 40
Device 41, bioreactor 40 are connected with zinc cation tower 20, for into zinc cation tower 20 supply cleaning solution with wash from
The gas being supplied in anaerobic reactor 10 in zinc cation tower 20, the cleaning solution after washing gas return to bioreactor 40
It is interior.Sulphur settling vessel 50 has inlet 51, liquid outlet 52 and elemental sulfur sludge outlet 53, inlet 51 and liquid outlet 52 and biology
Reactor 40 is connected, and a part for the cleaning solution discharged from bioreactor 40 is supplied in sulphur settling vessel 50 with from cleaning solution
Elemental sulfur is isolated, separator for mud and water 60 is connected with anaerobic reactor 10, for the row of delivery port 112 from anaerobic reactor 10
The mud mixture gone out is separated.
Thus, the Waste Water Treatment 1 of removal organic polluter and sulphur is removed while according to embodiments of the present invention, anaerobism is anti-
Device 10 is answered to be combined together with the biological desulphurization treatment apparatus of desulfurization process can be carried out, by reasonably designing, controlling stripping
The amount of hydrogen sulfide content and stripping biogas in biogas, the concentration of hydrogen sulfide in final waste water and biogas are up to a stabilization
Balance, enable removing COD in device and the continual and steady progress of desulphurization reaction, serve while remove removal organic polluter
With the effect of sulfate radical.
Below with reference to the accompanying drawings anaerobic reactor 10 according to embodiments of the present invention is described.
As shown in Figure 1-Figure 3, anaerobic reactor 10 according to embodiments of the present invention includes anaerobic fermentation tank body 100, air lift
Pipe 200 and air supply pipe 300.
There is anaerobic reaction room 110, anaerobic reaction room 110 has waste water inlet 111, water outlet in anaerobic fermentation tank body 100
Mouth 112 and exhaust outlet 113.The pipe of stripping tube 200 is located in anaerobic reaction room 110, and the upper end of stripping tube 200 has gas outlet 221,
And the lower end of stripping tube 200 has air inlet 211.Air supply pipe 300 is connected with the air inlet 211 of stripping tube 200, for air lift
The gas for air lift is supplied in pipe 200.The gas for being used for air lift can be oxygen-depleted gas or inert gas, preferably natural pond
Gas.
Below with reference to the accompanying drawings the anaerobic fermentation purification process of anaerobic reactor 10 according to embodiments of the present invention is described.
Waste water enters anaerobic reaction room 110 by waste water inlet 111, and air supply pipe 300 supplies to stripping tube 200, anaerobic reaction
Anaerobic environment is formed in room 110, meanwhile, stripping tube 200 plays stirring by exporting lift gas into anaerobic reaction room 110
The effect of waste water and anaerobic sludge, thus, the waste water in anaerobic reaction room 110 mix rapidly with anaerobic sludge, waste water and anaerobism
The intense contact of sludge makes the organic pollutant degradation in waste water, and the waste water after anaerobic fermentation purifies is flowed out by delivery port 112
Anaerobic reaction room 110, unnecessary gas is discharged by exhaust outlet 113 in anaerobic reaction room 110.
Anaerobic reactor 10 according to embodiments of the present invention, by setting stripping tube 200 and air supply pipe 300, it can utilize
Air supply pipe 300 provides gas into stripping tube 200, and can be entered using the output gas into anaerobic reaction room 110 of stripping tube 200
Promoting the circulation of qi carries, and the gas exported by stripping tube 200 can stir the mixture of the waste water and anaerobic sludge in anaerobic reaction room 110,
Waste water and anaerobic sludge is set to contact fully, rapidly, and stirring scope is big, mixing effect is good, can greatly improve COD processing effects
Fruit.
Also, by setting stripping tube 200, motor and stirring that air floating structure and air floating structure need to be equipped with can be cancelled
Element, the structure of anaerobic reactor 10 is simplified, reduce the cost of anaerobic reactor 10.
In addition, anaerobic reactor 10 according to embodiments of the present invention eliminates the motor that flotation cell and flotation cell need to be equipped with
And cleaning element, the structure of anaerobic reactor 10 is further simplify, and reduce further the cost of anaerobic reactor 10.
Anaerobic reactor 10 according to embodiments of the present invention, has that simple in construction, cost is low, COD high treating effects etc. are excellent
Point, can be by waste water using the cellulose alcohol wastewater processing system of anaerobic reactor 10 according to embodiments of the present invention
COD is handled to below 100mg/L.
Below with reference to the accompanying drawings anaerobic reactor 10 according to the specific embodiment of the invention is described.
As shown in Figure 1-Figure 3, anaerobic reactor 10 according to embodiments of the present invention includes anaerobic fermentation tank body 100, air lift
Pipe 200 and air supply pipe 300.
Advantageously, as shown in Figure 1 and Figure 2, the lower end of stripping tube 200 is adjacent to the bottom of anaerobic reaction room 110, and stripping tube
200 upper end extends to the top of anaerobic reaction room 110, and delivery port 112 is located at the top of anaerobic reaction room 110 and is higher than air lift
The upper end of pipe 200.The gas that air supply pipe 300 provides is transported to by the bottom of anaerobic reaction room 110 and detested by stripping tube 200
The top of oxygen reative cell 110, and exported from gas outlet 221 with to the waste water in anaerobic reaction room 110 and anaerobic sludge mixture
It is stirred, thus, can not only provides gas into stripping tube 200 in order to air supply pipe 300, and can further improve gas
Propose the stirring scope and mixing effect of pipe 200, and the water outlet by the gas that stripping tube 200 exports without interference with delivery port 112.
Alternatively, as shown in Figure 1 and Figure 2, the upper surface of stripping tube 200 is opened wide to form gas outlet 221, stripping tube 200
Lower surface is opened wide to form air inlet 211, can so increase air inlet 211 and effective stream of gas outlet 221 to greatest extent
Logical area, so as to improve the output quantity of gas in the unit interval of stripping tube 200.
In some specific embodiments according to the present invention, as shown in Figure 1 and Figure 2, stripping tube 200 includes the He of straight length 210
Segmental arc 220.Straight length 210 vertically extends, and segmental arc 220 is connected with the upper end of straight length 210, gas outlet 221
Angle α between opening direction and vertically downward direction is more than or equal to zero degree and is less than 180 degree, i.e. 180 ° of 0 °≤α ＜.
Preferably, as shown in Fig. 2 segmental arc 220 is inverted U-shaped, the opening direction of gas outlet 221 straight down, in other words,
α=0 °.So waste water and anaerobic sludge are stirred downwards from the top of anaerobic reaction room 110 by the gas that stripping tube 200 exports
Mixture, stirring scope and mixing effect are further increased, so as to further improve the COD processing effects of anaerobic reactor 10
Fruit.
The severe degree and speed mixed to further improve waste water with anaerobic sludge, stripping tube 200 can be
It is multiple, air supply pipe 300 can one or more and in anaerobic reaction room 110 bottom levels set, multiple stripping tubes 200 are in water
It is arranged at intervals in plane and lower end is connected with same air supply pipe 300 or is connected respectively with multiple air supply pipes 300.
In some specific examples of the present invention, as shown in Fig. 2 anaerobic reactor 10 also includes precipitation separator 400, sink
Shallow lake separator 400 is located in anaerobic reaction room 110 and positioned at the top of stripping tube 200, precipitation separator 400 has and delivery port
112 connected separator delivery ports 413.Waste water outflow after anaerobic fermentation purifies is in precipitation separator 400, thus gas
Separated with water and anaerobic sludge, the gas after separation is discharged by exhaust outlet 113, and then, water separates with anaerobic sludge, after separation
Anaerobic sludge is returned in anaerobic reaction room 110 from precipitation separator 400 and recycled, the separator delivery port 413 after separation
Delivery port 112 is transported to, discharge anaerobic reaction room 110 is simultaneously delivered to subsequent treatment process.
Gas, water and anaerobic sludge are first isolated thus, it is possible to be utilized in anaerobic reaction room 110 and precipitate separator 400,
Product after separation is each delivered to different regions again, improves the pure of water outlet.
Specifically, as shown in figure 3, precipitation separator 400 includes casing 410, dividing plate 420, precipitation inclined plate 430 and overflow
Weir 440.
Chamber 411 is precipitated formed with degassing in casing 410, the bottom of degassing precipitation chamber 411 has sludge outlet 412, deaerated
The cross-sectional area for precipitating the bottom of chamber 411 is gradually reduced along direction from the top down.Dividing plate 420 is located at degassing precipitation chamber 411
Top, will the deaerate top of precipitating chamber 411 of dividing plate 420 are separated into degassing district 421 and settling zone 422, the bottom of degassing district 421 with
The bottom of settling zone 422 is connected so that waste water overflows in degassing district 421 from anaerobic reaction room 110 and then from degassing district 421
Bottom is flowed in settling zone 422.Precipitation inclined plate 430 is located in settling zone 422.Downflow weir 440 is located in settling zone 422 and overflow
Weir 440 forms the overflow launder 441 with separator delivery port 413.
Separation process of the precipitation separator 400 to water, gas and anaerobic sludge is described below with reference to Fig. 3.
Gas-entrained and anaerobic sludge in water after anaerobic sludge is degraded, the gas-entrained and water overflow of anaerobic sludge is extremely
The degassing district 421 of degassing precipitation chamber 411, wherein gas are escaped from degassing district 421, discharged by exhaust outlet 113, complete gas point
From.The water of entrainment anaerobic sludge after being separated with gas flows to settling zone 422 by the bottom of degassing district 421, now anaerobic sludge
Precipitation is sunk and precipitated in degassing under the guiding of the inwall of the lower tilt of chamber 411 to sludge outlet 412, by the row of sludge outlet 412
Go out to precipitate separator 400 and enter anaerobic reaction room 110, continue on for wastewater degradation, in degassing precipitation chamber 411 and anaerobic sludge
In water overflow to the overflow launder 441 of downflow weir 440 after separation, and discharged successively by separator delivery port 413 and delivery port 112
Anaerobic reaction room 110, carry out subsequent treatment.During anaerobic sludge rises with water, anaerobic sludge settles on precipitation inclined plate 430
And degassing precipitation chamber 411 bottom is slipped to, contribute to anaerobic sludge to be separated from water, so far, complete water, anaerobic sludge and gas
Separation.
Advantageously, as shown in figure 3, limiting the upper edge of the casing 410 of degassing district 421 less than dividing plate 420 with dividing plate 420
Upper edge and limited with dividing plate 420 settling zone 422 the part of casing 410 upper edge.In other words, casing 410 limit it is de-
The upper edge of the part in gas area 421, less than edge on the part for limiting settling zone 422 of casing 410, and it is upper less than dividing plate 420
Edge.On downflow weir 440 along can with the part for limiting degassing district 421 of casing 410 along concordant or higher than casing 410
The part for limiting degassing district 421 upper edge, and the upper edge of downflow weir 440 limits settling zone 422 less than casing 410
Part on along and dividing plate 420 upper edge.The water in degassing district 421 be thus it can be prevented that from top overflow to settling zone 422,
Ensure that the water in degassing district 421 flow to settling zone 422 from the bottom of degassing district 421, and then be sufficiently separated anaerobic sludge, and sink
Water in shallow lake area 422 is by overflow to overflow launder 441, avoiding in the water in overflow launder 441 and carrying anaerobic sludge secretly.
Alternatively, as shown in figure 3, casing 410 is cuboid, the lower end of the first longitudinal side wall 414 of the bottom of casing 410 to
Under extend beyond casing 410 bottom the second longitudinal side wall 415 lower end, and the lower end of the first longitudinal side wall 414 and the second longitudinal side
The lower end of wall 415 is overlapping in the vertical direction.It is possible thereby to the anaerobic sludge in anaerobic reaction room 110 is advantageously avoided to pass through dirt
Mud outlet 412 enters in the degassing precipitation chamber 411 of precipitation separator 400.
For example, in four longitudinal side walls of casing 410, two longer longitudinal side walls of length are respectively in the horizontal direction
The lower end of one longitudinal side wall 414 and the second longitudinal side wall 415, the lower end of the first longitudinal side wall 414 and the second longitudinal side wall 415 is relative to first
The upper end of longitudinal side wall 414 and the upper end of the second longitudinal side wall 415 are mutually adjacent, and the lower end of the first longitudinal side wall 414 is located at the second longitudinal side
The lower section of the lower end of wall 415, and the projection of the lower end of the first longitudinal side wall 414 and the lower end of the second longitudinal side wall 415 in the horizontal plane
Overlapping, gap between the lower end of the lower end of the first longitudinal side wall 414 and the second longitudinal side wall 415 forms sludge outlet 412, and thus one
It is anti-that aspect can ensure that the anaerobic sludge in degassing precipitation chamber 411 can smoothly return to anaerobism by sludge outlet 412 after precipitating
Answer room 110, and on the other hand the structure of the sludge outlet 412 can stop anaerobic sludge in anaerobic reaction room 110 from sludge
Outlet 412 enters degassing precipitation chamber 411, ensures the anaerobic sludge separating effect of precipitation separator 400.
Advantageously, as shown in Figure 1 and Figure 2, anaerobic reactor 10 also includes water sealed tank 800, the top of anaerobic fermentation tank body 100
Portion is provided with safe gas port 114, and safe gas port 114 is connected with water sealed tank 800.It is possible thereby to completely cut off air, dimension using water sealed tank 800
The pressure of anaerobic reaction room 110 is held, and back-fire relief effect can be played, certain clean-up effect can be additionally played to biogas.
Alternatively it is also possible to water sealed tank 800 is replaced using safety valve.
Four units of technique point of hydrogen sulfide, including gas-liquid separator, zinc cation tower 20, life are removed from anaerobic methane
Thing reactor 40, sulphur settling vessel 50.Wherein, in order to which the solid particulate matter that removes the free water in biogas and may contain is miscellaneous
Matter, biogas need first enter the progress hydrogen sulfide stripping of zinc cation tower 20 after knockout drum.In this application, gas-liquid point
From process can be completed in anaerobic reactor 10, anaerobic reactor 10 may act as the effect of gas-liquid separation, by biogas
Free water removes.Biogas caused by anaerobic reactor 10 carries out removing hydrogen sulfide after gas-liquid separation into zinc cation tower 20
Reaction.
Biogas caused by anaerobic reactor 10 enters zinc cation tower 20 after gas-liquid separator, and biogas is in zinc cation tower
With top-down cleaning solution counter current contacting in 20, H during this2S be washed liquid absorb, purification (desulfurization) after biogas from
Gravity flow enters methane voltage-stabilizing cabinet 30 at the top of scrubbing tower.
Biogas gravity flow after being purified by biological desulfurization process enters methane voltage-stabilizing cabinet 30, and part biogas is pressurized by biogas
Blower fan, which returns, carries out biogas air lift stirring in anaerobic reactor 10, remaining biogas enters follow-up methane utilizing system or combustion
Burn.
Methane voltage-stabilizing cabinet 30 is made up of a cylinder of steel for having anticorrosive paint and a floating roof.Counterweight at the top of floating roof will be set
Gas system produces 2.5-3.0KPa gauge pressure, and floating roof is connected with tank body by the film of a telescopic polyester textile,
So floating roof can move up and down.So the volume of methane voltage-stabilizing cabinet 30 can increase or reduce without changing in gas system
Pressure.The gas position of methane voltage-stabilizing cabinet 30 is with pressure by level meter and pressure transmitter continuous monitoring.
Cleaning solution containing sulfide is flowed into bioreactor 40 from the bottom weight of zinc cation tower 20.Bioreactor
Contain Thiobacillus in 40 liquid phases, elemental sulfur is converted into this sulfide.Carrier without fixation of microbe in reactor, biological sulphur
The role of carrier is itself acted as.There is gas distribution system in bioreactor 40, oxygen is provided to microorganism by gas distribution system, with
Sulfide in reactor is converted into elemental sulfur, while alkali obtains bio-regeneration.
The mixed liquor circulated sprinkling containing bio-regeneration alkali is to zinc cation tower 20 in bioreactor 40, to remove anaerobism
Contained H in biogas2S。
A part of sludge of the elemental sulfur sludge outlet discharge of sulphur settling vessel 50 is returned in bioreactor 40.Specifically
Ground, some processes sulphur liquid are continuously pumped into sulphur settling vessel 50 by bioreactor 40, and the product sulfur separates with cleaning solution in the unit,
The product sulfur is delivered to Collection utilization after sludge treating system is handled by pump.
It is using the advantages of methane bio-desulfurization system：Alkali can be reclaimed from bioreactor 40, operating cost is low, and
And H2S clearances are high, anti-load impact such as tolerance change or H2The ability of S changes of contents is strong, and it is easy to start, and the time is short, automatic control
Simple system, it is easy to operate.
Aqueous vapor from the biogas saturation of biogas caused by anaerobic reactor 10 and biogas booster fan admission line, works as biogas
Water can condensation when temperature declines.These condensates are provided with extremely by being separated and collected in condensation water tank 70 in condensation water tank 70
The water seal of few 700mm depth is used to prevent the biogas from drainpipe leakage (draining comes from methane pipeline).The reclaimed water of condensation water tank 70
Sealing liquid position provides guarantee by a liquid-level switch and plant area's water system.
Due in biological desulphurization reactor using sulfur oxidizing bacterium, it is necessary to the temperature of maintenance reaction Qi Nei Institute of Micro-biology matters
Degree, and heat can be produced during biological desulphurization, biogas also has certain heat.Therefore devise and change on circulating-pump outlet
Hot device, the biological solution that this part is circulated is heated or cooled down if necessary, it is suitable in biological desulphurization reactor to ensure
Temperature.
Specifically, while the Waste Water Treatment 1 of removal organic polluter and sulphur is gone also to include First Heat Exchanger 80 and second
Heat exchanger 90, First Heat Exchanger 80 are used for the waste water being supplied to by waste water inlet 111 in anaerobic reactor 10 is carried out
Heat exchange.Second heat exchanger 90 is used to carry out heat with a part of cleaning solution for being supplied to zinc cation tower 20 from bioreactor 40
Exchange, the cleaning solution after heat exchange is returned in bioreactor 40, and also there is bioreactor 40 alkali lye and trace element to add
Entrance, the defoamer for adding defoamer add mouth.
The discharge opeing of bioreactor 40 drains into sulphur storage tank with the sulphur sludge of sulphur settling vessel 50 and kept in, and sulphur is squeezed into by sulphur charging pump
Dewatering system gives dewater treatment.Biogas biosystem sets alkali dosing pump to be used to add NaOH to bioreactor 40 to control
Its pH.
To prevent from producing excess foam in bioreactor 40, microorganism is caused to float and be lost in.Preferably, biological respinse
Part solution will be sprayed by circulating pump pump to the top of bioreactor 40 in device 40, and interface and defoaming are left on the pipeline
Agent adds unit and is connected, and is defoamed for additional defoamer.
In addition, bioreactor 40 also has moisturizing unit 401, moisturizing unit 401 can rinse zinc cation tower 20 and push up
The demister in portion, can with flush cycle pump line road, remaining sulphur sludge pump pipeline, sulphur sludge pump pipeline, prevent pipeline scale or
Block.The air of the blower export wind of bioreactor 40 can be cooled down simultaneously, prevent the medium temperature of bioreactor 40 from spending height.
Waste Water Treatment 1 that is according to an embodiment of the invention while removing removal organic polluter and sulphur, in addition to disappear
Energy device 61, sinker 61 is connected between anaerobic reactor 10 and separator for mud and water 60, for being supplied from anaerobic reactor 10
Mud mixture to separator for mud and water 60 carries out energy dissipating, it is preferable that sinker 61 has the exhaust outlet with anaerobic reactor 10
113 connected gas outlets 611.
As shown in figure 4, the Waste Water Treatment 1 of removal organic polluter and sulphur is gone also to include sinker 61, sinker simultaneously
61 are connected between the delivery port 112 of anaerobic reaction room 110 and separator for mud and water 60.So can utilize sinker 61 consumption and
The energy of the scattered water flowed out by anaerobic fermentation tank body 100, prevents or mitigates the water flowed out by anaerobic fermentation tank body 100 to muddy water
The erosion damage of separator 60.In addition, the structure of separator for mud and water 60 can be with above-mentioned precipitation separator 400 with connected mode
Structure is similar with connected mode, therefore is not described in detail.
In certain specific embodiments of the invention, sludge outlet and the phase of anaerobic reactor 10 of separator for mud and water 60
Even, a part of sludge discharged from separator for mud and water 60 is supplied in anaerobic reactor 10, and anaerobic reactor 10 also has residue
Sludge outlet.
Advantageously, as shown in figure 4, anaerobic reactor 10 also includes mud return line 600, one end of mud return line 600
Connected with anaerobic reaction room 110, the sludge outlet of separator for mud and water 60 passes through sludge discharge pipe 700 and the phase of mud return line 600
Even, mud return line 600 is provided with sludge reflux pump, and sludge discharge can be passed sequentially through from the anaerobic sludge of sludge outlet discharge
Pipe 700 and mud return line 600 return to anaerobic reaction room 110, so as to be recycled.
In the description of the invention, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", " on ", " under ", "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom " " interior ", " outer ", " up time
The orientation or position relationship of the instruction such as pin ", " counterclockwise ", " axial direction ", " radial direction ", " circumference " be based on orientation shown in the drawings or
Position relationship, it is for only for ease of and describes the present invention and simplify description, rather than indicates or imply that signified device or element must
There must be specific orientation, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are only used for describing purpose, and it is not intended that instruction or hint relative importance
Or the implicit quantity for indicating indicated technical characteristic.Thus, define " first ", the feature of " second " can be expressed or
Implicitly include at least one this feature.In the description of the invention, " multiple " are meant that at least two, such as two, three
It is individual etc., unless otherwise specifically defined.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation " etc.
Term should be interpreted broadly, for example, it may be fixedly connected or be detachably connected, or integrally；Can be that machinery connects
Connect or electrically connect or can communicate each other；Can be joined directly together, can also be indirectly connected by intermediary, can be with
It is connection or the interaction relationship of two elements of two element internals, is limited unless otherwise clear and definite.For this area
For those of ordinary skill, the concrete meaning of above-mentioned term in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature can be with "above" or "below" second feature
It is that the first and second features directly contact, or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature are directly over second feature or oblique upper, or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward, or is merely representative of fisrt feature level height and is less than second feature.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment or example of the present invention.In this manual, to the schematic representation of above-mentioned term not
Identical embodiment or example must be directed to.Moreover, specific features, structure, material or the feature of description can be with office
Combined in an appropriate manner in one or more embodiments or example.In addition, in the case of not conflicting, the skill of this area
Art personnel can be tied the different embodiments or example and the feature of different embodiments or example described in this specification
Close and combine.
Although embodiments of the invention have been shown and described above, it is to be understood that above-described embodiment is example
Property, it is impossible to limitation of the present invention is interpreted as, one of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changed, replacing and modification.
Claims (10)
1. Waste Water Treatment that is a kind of while removing removal organic polluter and sulphur, it is characterised in that including：
Anaerobic reactor, the anaerobic reactor include anaerobic reaction room, stripping tube and air supply pipe, and the anaerobic reaction room has
Waste water inlet, delivery port and exhaust outlet, the stripping tube are located in the anaerobic reaction room, and the upper end of the stripping tube has
The lower end of gas port and the stripping tube has air inlet, and the air supply pipe is connected with the air inlet of the stripping tube, for institute
State the gas supplied in stripping tube for air lift；
Zinc cation tower, the zinc cation tower are connected with the exhaust outlet of the anaerobic reactor, for anti-from the anaerobism
The gas for answering device to discharge is washed；
Methane voltage-stabilizing cabinet, the methane voltage-stabilizing cabinet is connected with the air inlet of the zinc cation tower and the stripping tube, for steady
Press the biogas from zinc cation tower discharge and a part of biogas is supplied in the stripping tube；
Bioreactor, the bioreactor is interior to be provided with aerator, the bioreactor and the zinc cation tower phase
Even, the zinc cation is supplied to out of described anaerobic reactor to wash for supplying cleaning solution into the zinc cation tower
Gas in tower, the cleaning solution after washing gas are returned in the bioreactor；
Sulphur settling vessel, the sulphur settling vessel have inlet, liquid outlet and an elemental sulfur sludge outlet, the inlet and it is described go out
Liquid mouth is connected with the bioreactor, and the sulphur precipitation is supplied to from a part for the cleaning solution of bioreactor discharge
To isolate elemental sulfur from cleaning solution in device；With
Separator for mud and water, the mud-water separation separator for mud and water are connected with the anaerobic reactor, for anti-from the anaerobism
The mud mixture for answering the delivery port of device to discharge is separated.
2. Waste Water Treatment that is according to claim 1 while removing removal organic polluter and sulphur, it is characterised in that also wrap
Sinker is included, the sinker is connected between the anaerobic reactor and the separator for mud and water, for from the anaerobism
The mud mixture that reactor is supplied to the separator for mud and water carries out energy dissipating.
3. Waste Water Treatment that is according to claim 2 while removing removal organic polluter and sulphur, it is characterised in that described
Sinker has the gas outlet being connected with the exhaust outlet of the anaerobic reactor.
4. Waste Water Treatment that is according to claim 2 while removing removal organic polluter and sulphur, it is characterised in that described
The sludge outlet of separator for mud and water is connected with the anaerobic reactor, from a part of sludge supply of separator for mud and water discharge
Into the anaerobic reactor, the anaerobic reactor also has excess sludge outlet.
5. Waste Water Treatment that is according to claim 1 while removing removal organic polluter and sulphur, it is characterised in that also wrap
First Heat Exchanger is included, the First Heat Exchanger is used for will be supplied to by the waste water inlet in the anaerobic reactor
Waste water carries out heat exchange.
6. Waste Water Treatment that is according to claim 1 while removing removal organic polluter and sulphur, it is characterised in that also wrap
The second heat exchanger is included, second heat exchanger is used for the part with being supplied to the zinc cation tower from the bioreactor
Cleaning solution carries out heat exchange, and the cleaning solution after heat exchange is returned in the bioreactor, and the bioreactor also has
Alkali lye and trace element add mouth, and the defoamer for adding defoamer adds mouth.
7. Waste Water Treatment that is according to claim 1 while removing removal organic polluter and sulphur, it is characterised in that described
A part of sludge of the elemental sulfur sludge outlet discharge of sulphur settling vessel is returned in the bioreactor.
8. removing the Waste Water Treatment of removal organic polluter and sulphur while according to any one of claim 1-7, it is special
Sign is that the anaerobic reactor also includes precipitation separator, and the precipitation separator is located in the anaerobic reaction room and position
Above the stripping tube, the precipitation separator has the separator delivery port being connected with the delivery port.
9. Waste Water Treatment that is according to claim 8 while removing removal organic polluter and sulphur, it is characterised in that described
Precipitation separator includes：
Casing, the casing is interior to precipitate chamber formed with degassing, and the bottom of the degassing precipitation chamber has sludge outlet, the degassing
The cross-sectional area for precipitating the bottom of chamber is gradually reduced along direction from the top down；
Dividing plate, the dividing plate be located at it is described degassing precipitation chamber top, the dividing plate by it is described degassing precipitate chamber upper part every
Into degassing district and settling zone, the bottom of the degassing district is connected with the bottom of the settling zone so that waste water is from the anaerobic reaction
Room overflows in the degassing district and then flowed to from the bottom of the degassing district in the settling zone；
Precipitation inclined plate, the precipitation inclined plate are located in the settling zone；
Downflow weir, the downflow weir is located in the settling zone and the downflow weir forms overflowing with the separator delivery port
Chute.
10. Waste Water Treatment that is according to claim 9 while removing removal organic polluter and sulphur, it is characterised in that with
The upper edge that the dividing plate limits the box portion of the degassing district limits less than the upper edge of the dividing plate and with the dividing plate
Go out the upper edge of the box portion of the settling zone, the casing is cuboid, under the first longitudinal side wall of the bottom of the casing
End extends downward beyond the lower end of the second longitudinal side wall of the bottom of the casing, and the lower end of first longitudinal side wall and described the
The lower end of two longitudinal side walls is overlapping in the vertical direction.
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| CN115124189A (en) * | 2022-06-24 | 2022-09-30 | 上海康恒环境股份有限公司 | Reactor for removing heavy metal and preventing scale in leachate |
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