CN107540148A - The method of wastewater treatment of the Waste Water Treatment sum of cellulose ethanol - Google Patents
The method of wastewater treatment of the Waste Water Treatment sum of cellulose ethanol Download PDFInfo
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- CN107540148A CN107540148A CN201610464935.4A CN201610464935A CN107540148A CN 107540148 A CN107540148 A CN 107540148A CN 201610464935 A CN201610464935 A CN 201610464935A CN 107540148 A CN107540148 A CN 107540148A
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- waste water
- dephosphorization
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- precipitation
- degassing
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 146
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 70
- 239000001913 cellulose Substances 0.000 title claims abstract description 68
- 229920002678 cellulose Polymers 0.000 title claims abstract description 68
- 238000006243 chemical reaction Methods 0.000 claims abstract description 246
- 239000002351 wastewater Substances 0.000 claims abstract description 164
- 238000001556 precipitation Methods 0.000 claims abstract description 127
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 114
- 238000007872 degassing Methods 0.000 claims abstract description 103
- 238000000855 fermentation Methods 0.000 claims abstract description 64
- 239000007789 gas Substances 0.000 claims abstract description 63
- 230000008569 process Effects 0.000 claims abstract description 37
- 238000005276 aerator Methods 0.000 claims abstract description 26
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 13
- 239000010802 sludge Substances 0.000 claims description 112
- 238000000926 separation method Methods 0.000 claims description 37
- 239000002244 precipitate Substances 0.000 claims description 15
- 238000001727 in vivo Methods 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 28
- YUWBVKYVJWNVLE-UHFFFAOYSA-N [N].[P] Chemical compound [N].[P] YUWBVKYVJWNVLE-UHFFFAOYSA-N 0.000 abstract description 9
- 238000010276 construction Methods 0.000 abstract description 6
- 238000005273 aeration Methods 0.000 description 47
- 238000004062 sedimentation Methods 0.000 description 31
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 24
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 description 24
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 19
- 229910052698 phosphorus Inorganic materials 0.000 description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 16
- 238000005189 flocculation Methods 0.000 description 16
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- 238000012545 processing Methods 0.000 description 16
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- 230000008676 import Effects 0.000 description 11
- 230000003647 oxidation Effects 0.000 description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 239000001301 oxygen Substances 0.000 description 9
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- 238000003756 stirring Methods 0.000 description 9
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- 229910021529 ammonia Inorganic materials 0.000 description 8
- 238000005345 coagulation Methods 0.000 description 8
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- 238000005516 engineering process Methods 0.000 description 8
- SURQXAFEQWPFPV-UHFFFAOYSA-L iron(2+) sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Fe+2].[O-]S([O-])(=O)=O SURQXAFEQWPFPV-UHFFFAOYSA-L 0.000 description 7
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 6
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 6
- 229910001882 dioxygen Inorganic materials 0.000 description 6
- 239000003337 fertilizer Substances 0.000 description 6
- 238000007667 floating Methods 0.000 description 6
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- 238000004519 manufacturing process Methods 0.000 description 6
- 238000006396 nitration reaction Methods 0.000 description 6
- 230000001376 precipitating effect Effects 0.000 description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 5
- 238000006065 biodegradation reaction Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
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- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 3
- 240000003183 Manihot esculenta Species 0.000 description 3
- 235000016735 Manihot esculenta subsp esculenta Nutrition 0.000 description 3
- 229910019142 PO4 Inorganic materials 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 240000008042 Zea mays Species 0.000 description 3
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 3
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 3
- 230000001112 coagulating effect Effects 0.000 description 3
- 235000005822 corn Nutrition 0.000 description 3
- 238000012851 eutrophication Methods 0.000 description 3
- 210000003608 fece Anatomy 0.000 description 3
- 239000011790 ferrous sulphate Substances 0.000 description 3
- 235000003891 ferrous sulphate Nutrition 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000395 magnesium oxide Substances 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 3
- 239000010452 phosphate Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000009287 sand filtration Methods 0.000 description 3
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 206010021143 Hypoxia Diseases 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
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- 150000002500 ions Chemical class 0.000 description 2
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- 238000012360 testing method Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 1
- 241000220317 Rosa Species 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
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- 238000012512 characterization method Methods 0.000 description 1
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- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
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- 229910052567 struvite Inorganic materials 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- AAKBLFQBZDFKMP-UHFFFAOYSA-H trimagnesium azane diphosphate Chemical compound N.[Mg+2].[Mg+2].[Mg+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O AAKBLFQBZDFKMP-UHFFFAOYSA-H 0.000 description 1
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Abstract
The invention discloses a kind of Waste Water Treatment and method of wastewater treatment of cellulose ethanol, the Waste Water Treatment of the cellulose ethanol includes anaerobic fermentation reaction unit, waste water dephosphorization reaction unit, denitrification reactor and the advanced treatment system that waste water treatment process direction is sequentially connected, wherein, the anaerobic fermentation reaction unit includes anaerobic fermentation tank body, stripping tube and air supply pipe, the stripping tube is located in the anaerobic reaction room, and lower end of the upper end of the stripping tube with gas outlet and the stripping tube is with air inlet；The waste water dephosphorization reaction unit includes dephosphorization reacting tank body, aerator and degassing precipitation separator, there is dephosphorization reative cell in the dephosphorization reacting tank body, the dephosphorization reative cell has water inlet and dephosphorization agent adding mouth, and the aerator is located in the dephosphorization reative cell.The Waste Water Treatment of cellulose ethanol according to embodiments of the present invention has the advantages that simple in construction, cost is low, COD and nitrogen phosphorus high treating effect.
Description
Technical field
The present invention relates to environmental technology field, in particular to a kind of Waste Water Treatment and fiber of cellulose ethanol
The method of wastewater treatment of element ethanol.
Background technology
Traditional ethanol method of manufacturing technology, using corn, cassava (i.e. starch) by ferment etc. obtained ethanol, waste water
For COD (organic pollution) generally between 2,000 to 3,000, processing is easy.But because corn, cassava cost are higher, raw material
Limited, this kind of ethanol method of manufacturing technology has been prohibited.
Therefore, proposed in correlation technique with the process that straw, stalk (cellulose) are raw material manufacture ethanol, for
For straw, stalk, cellulose inside it is coated by outer wood element, therefore needs to incite somebody to action by HTHP or sulfuric acid first
The lignin explosion of outer layer, saccharification ethanol is carried out after exposing the cellulose of inside, the COD of waste water is generally 50,000 to 90,000
Between, relative difficulty is handled, the complicated and cost of sewage treatment equipment is higher, and COD and nitrogen phosphorus treatment effect are bad,
Improved demand be present.
The content of the invention
It is contemplated that at least solves one of above-mentioned technical problem in correlation technique to a certain extent.Therefore, the present invention carries
Go out a kind of Waste Water Treatment of cellulose ethanol, the Waste Water Treatment of the cellulose ethanol have it is simple in construction, into
This low, COD and the advantages that nitrogen phosphorus high treating effect.
The present invention also propose it is a kind of can simplied system structure, reduce cost, improve COD treatment effects cellulose ethanol
Method of wastewater treatment.
To achieve the above object, embodiment according to the first aspect of the invention proposes a kind of wastewater treatment of cellulose ethanol
System, the Waste Water Treatment of the cellulose ethanol include the anaerobic fermentation reaction that waste water treatment process direction is sequentially connected
Device, waste water dephosphorization reaction unit, denitrification reactor and advanced treatment system, wherein, the anaerobic fermentation reaction unit bag
Anaerobic fermentation tank body, stripping tube and air supply pipe are included, there is anaerobic reaction room, the anaerobic reaction in the anaerobic fermentation tank body
Room has waste water inlet, delivery port and exhaust outlet, and the stripping tube is located in the anaerobic reaction room, the stripping tube it is upper
Lower end of the end with gas outlet and the stripping tube is connected with air inlet, the air supply pipe with the air inlet of the stripping tube,
For supplying the gas for air lift into the stripping tube；The waste water dephosphorization reaction unit includes dephosphorization reacting tank body, exposed
Device of air and degassing precipitation separator, have dephosphorization reative cell in the dephosphorization reacting tank body, the dephosphorization reative cell have into
The mouth of a river and dephosphorization agent adding mouth, the aerator are located in the dephosphorization reative cell, and the degassing precipitation separator is located at institute
State in dephosphorization reative cell and above the aerator, for separating gas and water and sludge.
The Waste Water Treatment of cellulose ethanol according to embodiments of the present invention has that simple in construction, cost is low, COD and nitrogen phosphorus
The advantages that high treating effect.
In addition, the Waste Water Treatment of cellulose ethanol according to embodiments of the present invention can also have technology additional as follows
Feature：
According to one embodiment of present invention, the lower end of the stripping tube is adjacent to the bottom of the anaerobic reaction room and the air lift
The upper end of pipe extends to the top of the anaerobic reaction room, and the delivery port is located at the top of the anaerobic reaction room and is higher than institute
State the upper end of stripping tube.
According to one embodiment of present invention, the upper surface of the stripping tube is opened wide to form the gas outlet, the stripping tube
Lower surface open wide to form the air inlet.
According to one embodiment of present invention, the stripping tube include the straight length that vertically extends and with the straight length
The connected segmental arc in upper end, the angle between the opening direction and vertically downward direction of the gas outlet is more than or equal to zero degree
And it is less than 180 degree.
According to one embodiment of present invention, the segmental arc is inverted U-shaped that the opening direction of the gas outlet is straight down.
According to one embodiment of present invention, the stripping tube is multiple and is arranged at intervals in the horizontal plane.
According to one embodiment of present invention, the anaerobic fermentation reaction unit also includes：Precipitate separator, the precipitation point
It is located at from device in the anaerobic reaction room and above the stripping tube, the precipitation separator has and the delivery port phase
Separator delivery port and the delivery port even is connected with the water inlet of the waste water dephosphorization reaction unit.
According to one embodiment of present invention, the precipitation separator includes：Casing, the casing is interior to be precipitated formed with degassing
Chamber, the bottom of the degassing precipitation chamber have sludge outlet, and the cross-sectional area of the bottom of the degassing precipitation chamber is along from the top down
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 overflow
Weir forms the overflow launder with the separator delivery port.
According to one embodiment of present invention, the upper edge of the box portion of the degassing district is limited with the dividing plate less than described
The upper edge of dividing plate and the upper edge that the box portion of the settling zone is limited with the dividing plate.
According to one embodiment of present invention, the casing is cuboid, the lower end of the first longitudinal side wall of the bottom of the casing
Extend 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 second
The lower end of longitudinal side wall is overlapping in the vertical direction.
According to one embodiment of present invention, the anaerobic fermentation reaction unit also includes：Precipitate separator, the precipitation point
It is located at that the anaerobic fermentation tank is external and the delivery port passes through the precipitation separator and the waste water dephosphorization reaction unit from device
It is connected, the precipitation separator includes：Casing, forms degassing precipitation chamber in the casing, the degassing precipitation chamber have into
Mouth, separator delivery port and sludge outlet, the import connect with the delivery port, and the separator delivery port gives up with described
Water dephosphorization reaction unit is connected, and the bottom of the degassing precipitation chamber is formed as cross-sectional area and is gradually reduced along direction from the top down
At least one conical cavity, the sludge outlet formed in the bottom of the conical cavity；Precipitation inclined plate, the precipitation inclined plate are set
In the degassing precipitation intracavitary；Downflow weir, the downflow weir be located at it is described degassing precipitation intracavitary and the downflow weir in formed with
The overflow launder connected with the separator delivery port.
According to one embodiment of present invention, the anaerobic fermentation reaction unit also includes：Sinker, the sinker connection
Between the import of the delivery port and the degassing precipitation chamber of the anaerobic reaction room.
According to one embodiment of present invention, the anaerobic fermentation reaction unit also includes：For will be arranged from the sludge outlet
The mud return line that the sludge gone out is returned in the anaerobic reaction room, one end of the mud return line and the anaerobic reaction
Room is connected, and the sludge outlet is connected by sludge discharge pipe with the mud return line, and the mud return line is provided with sludge
Reflux pump.
According to one embodiment of present invention, the anaerobic fermentation reaction unit also includes：Water sealed tank, the anaerobic fermentation tank
The top of body is provided with safe gas port, and the safe gas port is connected with the water sealed tank.
According to one embodiment of present invention, the aerator has spaced multiple aeration heads or aeration tube.
According to one embodiment of present invention, the waste water dephosphorization reaction unit also includes：Multiple guide shells, it is each described to lead
The top and bottom of flow cartridge are opened wide, and the multiple aeration heads or aeration tube stretch into more from the lower end of multiple guide shells respectively
The individual guide shell.
According to one embodiment of present invention, waste water dephosphorization reaction unit also includes：It is located in the dephosphorization reative cell and is located at
Water-locator below the aerator, the water-locator are connected with the water inlet.
According to one embodiment of present invention, multiple water distribution mouths that the water-locator has interval setting and Open Side Down.
According to one embodiment of present invention, the dephosphorization reative cell has the discharge gate positioned at the dephosphorization reacting tank body bottom.
According to one embodiment of present invention, waste water dephosphorization reaction unit also includes：Cyclone, the cyclone have eddy flow
Device import, mud mouth and cyclone outlet, the cyclone inlets connect with the discharge gate, and the cyclone outlet passes through
Return pipe is connected with the dephosphorization reative cell.
According to one embodiment of present invention, the waste water dephosphorization reaction unit also includes：Pump and the desliming device being connected with pump,
Clear liquid after the desliming device removing sludge returns to the dephosphorization reative cell.
According to one embodiment of present invention, the waste water dephosphorization reaction unit also includes：Pump and the precipitation being connected with the pump
Device, the stillness of night after the settler precipitates return to the dephosphorization reative cell.
According to one embodiment of present invention, the degassing precipitation separator includes：Separator body, the separator body
Interior to form the mud chamber that deaerates, there is sludge to arrange mouth for the bottom of the degassing precipitation chamber, and the degassing precipitates the transversal of the bottom of chamber
Area is gradually reduced along direction from the top down；Baffle plate, the baffle plate are located at the top of the degassing mud chamber, the baffle plate
The top of the degassing mud chamber is separated into devolatilizing chamber and precipitation chamber, the bottom of the devolatilizing chamber and the bottom of the precipitation chamber
Connection overflows in the devolatilizing chamber from the dephosphorization reative cell so as to waste water and then flows to described sink from the bottom of the devolatilizing chamber
Shallow lake intracavitary；Inclined settling plate tilts sediment tube, and the inclined settling plate or inclination sediment tube are located at the precipitation intracavitary；Go out
Water downflow weir, the effluent overflow weir water is located at the precipitation intracavitary and the effluent overflow weir water is formed to have and connected with denitrification reactor
The water outlet overflow launder of logical separation outlet.
According to one embodiment of present invention, limited with the baffle plate separator body part of the devolatilizing chamber on along low
In the upper edge of the baffle plate and with the baffle plate limit it is described precipitation chamber separator body part upper edge.
According to one embodiment of present invention, the cross section of the separator body is rectangle.
According to one embodiment of present invention, the lower end of the first longitudinal side wall of the bottom of the separator body extends downward beyond
The lower end of second longitudinal side wall of the bottom of the separator body, and the lower end of first longitudinal side wall and second longitudinal side wall
Lower end it is overlapping in the vertical direction.
According to one embodiment of present invention, the waste water dephosphorization reaction unit also includes：It is located at outside the dephosphorization reacting tank body
The portion and aeration pump or Aeration fan being connected with the aerator, the water inlet are connected with waste water control valve.
According to one embodiment of present invention, the top of the dephosphorization reacting tank body is provided with top cover, and the dephosphorization agent adding mouth is set
On the top cover.
According to one embodiment of present invention, the denitrification reactor includes anaerobic ammonia oxidation reactor and the anoxic being connected to each other
Aerobic reaction tank.
According to one embodiment of present invention, in addition to coagulation reaction device, the coagulation reaction device are connected to the denitrogenation
Between reactor and the advanced treatment system, the coagulation reaction device has to be connected successively along the waste water treatment process direction
Logical coagulating basin, flocculation basin and sedimentation basin.
According to one embodiment of present invention, the advanced treatment system includes being sequentially connected along the waste water treatment process direction
Multigroup Fenton's reaction device, every group of Fenton's reaction device include Fenton's reaction pond and Fenton sedimentation basin.
According to one embodiment of present invention, have in each Fenton's reaction pond along the waste water treatment process direction successively
Multiple Fenton's reaction chambers and Fenton the flocculation chamber of connection, each Fenton's reaction intracavitary are provided with the fast mixer of Fenton and the sweet smell
Flocculation intracavitary of pausing is provided with the slow mixer of Fenton, and Fenton tilted plate separator and Fenton mud scraper are provided with each Fenton sedimentation basin.
According to one embodiment of present invention, the advanced treatment system also includes：Sand filter, the sand filter give up along described
It is connected on water treatment technology direction with Fenton sedimentation basin last described；Air reservoir, the air reservoir and the sand filtration
Device is connected.
According to one embodiment of present invention, multiple Fenton's reaction ponds include one-level Fenton's reaction pond and two level Fenton's reaction
Pond, multiple Fenton sedimentation basins include one-level Fenton sedimentation basin and two level Fenton sedimentation basin, the one-level Fenton's reaction pond,
The one-level Fenton sedimentation basin, the two level Fenton's reaction pond and the two level Fenton sedimentation basin are along the waste water treatment process side
To being sequentially connected.
According to one embodiment of present invention, the advanced treatment system also includes：Sulfuric acid storage tank, the sulfuric acid storage tank with it is every
Being connected along first on the waste water treatment process direction in multiple Fenton's reaction chambers in the individual Fenton's reaction pond；Sulfuric acid
Ferrous iron solution tank, the copperas solution tank and being given up along described in multiple Fenton's reaction chambers in each Fenton's reaction pond
First on water treatment technology direction is connected；Dioxygen water storage tank, the dioxygen water storage tank and each Fenton's reaction pond
Being connected along first on the waste water treatment process direction in multiple Fenton's reaction chambers；Fenton flocculant tank, the Fenton
Flocculation tank is connected with the Fenton flocculation chamber in each Fenton's reaction pond.
Embodiment according to the second aspect of the invention proposes a kind of method of wastewater treatment of cellulose ethanol, the cellulose
The method of wastewater treatment of ethanol processed comprises the following steps：
A：Waste water is carried out under anaerobic environment biodegradable；
B：Waste water after biodegradation is aerated and dephosphorization；
C：Denitrogenation is carried out to the waste water after aeration and dephosphorization；
D：Depths processing is carried out to the waste water after denitrogenation, so that further removal can not biodegradable organic pollution.
The method of wastewater treatment of cellulose ethanol according to embodiments of the present invention can simplied system structure, reduce cost, carry
High COD and nitrogen phosphorus treatment effect.
According to one embodiment of present invention, in the step A, the compressed biogas flowed from the bottom to top is passed through, so that useless
Water and sludge fully contact.
According to one embodiment of present invention, in the step A, precipitation is de-gassed to the waste water after biodegradation
Separation, the step B is carried out to the waste water after degassed precipitation separation.
According to one embodiment of present invention, in the step B, it is passed through air and is aerated, and adds magnesia conduct
Dephosphorization agent.
According to one embodiment of present invention, the step C includes following sub-step：
C1：Anammox reaction is carried out to the waste water after aeration and dephosphorization；
C2：To carrying out anti-nitration reaction by the reacted waste water of Anammox under anaerobic environment；
C3：To carrying out nitration reaction by the waste water of anti-nitration reaction under aerobic environment.
According to one embodiment of present invention, after the step C, coagulation first is carried out to the waste water after denitrogenation, then carry out institute
State step D.
According to one embodiment of present invention, the step D includes following sub-step：
D1：One-level Fenton's reaction is carried out to the waste water after denitrogenation；
D2：One-level degassing precipitation separation is carried out to the waste water by one-level Fenton's reaction；
D3：Waste water after the precipitation that deaerated to one-level separation carries out two level Fenton's reaction；
D4：Two level degassing precipitation separation is carried out to the waste water after two level Fenton's reaction；
D5：Sand filtration is carried out to the waste water after two level deaerates precipitation separation.
According to one embodiment of present invention, sulfuric acid, ferrous sulfate are added respectively in the step D1 and the step D4
It is stirred with hydrogen peroxide, then adds flocculant and be stirred.
Brief description of the drawings
Fig. 1 is the structural representation of the Waste Water Treatment of cellulose ethanol according to embodiments of the present invention.
Fig. 2 is the structure of the anaerobic fermentation reaction unit of the Waste Water Treatment of cellulose ethanol according to embodiments of the present invention
Schematic diagram.
Fig. 3 is the structure of the waste water dephosphorization reaction unit of the Waste Water Treatment of cellulose ethanol according to embodiments of the present invention
Schematic diagram.
Fig. 4 is the degassing of the waste water dephosphorization reaction unit of the Waste Water Treatment of cellulose ethanol according to embodiments of the present invention
Precipitate cyclone separator arrangement schematic diagram.
Fig. 5 is the structural representation according to the Waste Water Treatment of the cellulose ethanol of the first alternative embodiment of the invention.
Fig. 6 is to react dress according to the anaerobic fermentation of the Waste Water Treatment of the cellulose ethanol of the first alternative embodiment of the invention
The structural representation put.
Fig. 7 is to react dress according to the anaerobic fermentation of the Waste Water Treatment of the cellulose ethanol of the first alternative embodiment of the invention
The precipitation cyclone separator arrangement schematic diagram put.
Fig. 8 is the structural representation according to the Waste Water Treatment of the cellulose ethanol of the second alternative embodiment of the invention.
Fig. 9 is to react dress according to the anaerobic fermentation of the Waste Water Treatment of the cellulose ethanol of the second alternative embodiment of the invention
The structural representation put.
Figure 10 is the structural representation according to the Waste Water Treatment of the cellulose ethanol of the 3rd alternative embodiment of the invention.
Figure 11 is to react dress according to the anaerobic fermentation of the Waste Water Treatment of the cellulose ethanol of the 3rd alternative embodiment of the invention
The structural representation put.
Reference：
The Waste Water Treatment 1 of cellulose ethanol,
Anaerobic fermentation reaction unit 10, waste water dephosphorization reaction unit 20, denitrification reactor 40, advanced treatment system 60,
Anaerobic fermentation tank body 100, anaerobic reaction room 110, waste water inlet 111, delivery port 112, exhaust outlet 113, substitute
Mouthfuls 114, mud discharging mouth 115, mud discharging valve and/or mud discharging pump 116, charging pump 117, gas control valve 118,
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, import 416, dividing plate 420, degassing district 421, settling zone 422, precipitation inclined plate
430th, downflow weir 440, overflow launder 441,
Sinker 500,
Mud return line 600, sludge reflux pump 610,
Sludge discharge pipe 700,
Water sealed tank 800,
Dephosphorization reacting tank body 1100, dephosphorization reative cell 1110, water inlet 1111, dephosphorization agent adding mouth 1112, discharge gate 1113,
Waste water control valve 1114, top cover 1115, blow-off valve 1116,
Aerator 1200, aeration head or aeration tube 1210,
Degassing precipitation separator 1300, separator body 1310, degassing mud chamber 1311, devolatilizing chamber 1312, precipitation chamber 1313,
Sludge row mouth 1314, the first longitudinal side wall 1315, the second longitudinal side wall 1316, baffle plate 1320, inclined settling plate tilt precipitation
Pipe 1330, effluent overflow weir water 1340, water outlet overflow launder 1341, separation outlet 1342,
Guide shell 1400,
Water-locator 1500, water distribution mouth 1510,
Cyclone 1600, cyclone inlets 1610, mud mouth 1620, cyclone outlet 1630, return pipe 1640,
Aeration pump or Aeration fan 1700,
Anaerobic ammonia oxidation reactor 2100, Anoxic/Aerobic reaction tank 2200,
Fenton's reaction device 4100, one-level Fenton's reaction pond 4110, two level Fenton's reaction pond 4120, Fenton's reaction chamber 4111,
Fenton flocculation chamber 4112, the fast mixer 4113 of Fenton, the slow mixer 4114 of Fenton, one-level Fenton sedimentation basin 4130, two level
Fenton sedimentation basin 4140, Fenton tilted plate separator 4131, Fenton mud scraper 4132, sand filter 4200, air reservoir 4300,
Sulfuric acid storage tank 4400, copperas solution tank 4500, dioxygen water storage tank 4600, Fenton flocculant tank 4700.
Embodiment
Embodiments of the invention are described below in detail, the example of the embodiment is shown in the drawings, wherein identical from beginning to end
Or similar label represents same or similar element or the element with same or like function.Retouched below with reference to accompanying drawing
The embodiment stated is exemplary, it is intended to for explaining the present invention, and is not considered as limiting the invention.
As the process using corn, cassava (i.e. starch) manufacture ethanol is prohibited, with straw, stalk (cellulose)
The process that ethanol is manufactured for raw material obtains more and more extensive application, but cellulose ethanol compares traditional starch second
Alcohol, the COD from 2,000 to 3,000 in waste water rise to 50,000 to 90,000, and the difficulty of wastewater treatment also accordingly increases.
The Waste Water Treatment of cellulose ethanol in correlation technique, not only COD treatment effects are limited, can not be by waste water
COD processing to below 100mg/L, and tedious process, system forms complicated, and cost is higher.
Specifically, for the waste water treatment process of cellulose ethanol, anaerobic fermentation purification is necessary process, is passed through
The process is degraded in the presence of anaerobic organism to the organic pollution in waste water.
Existing anaerobic fermentation reaction unit is typically provided with air floating structure, such as sets upper and lower ends to open in anaerobic reaction chamber interior
The body opened, and motor and the agitating element being connected with motor, driving backspin of the agitating element in motor are set in body
Turn and push down on current, to form downward current in body, thus, waste water and sludge in anaerobic reaction room it is mixed
Compound enters from body upper end and flowed out from anaerobic fermentation tank body lower end, forms circulation.
In addition, existing anaerobic fermentation reaction unit also generally sets flotation cell in anaerobic reaction room, and flotation cell is upper and lower
Both ends are respectively equipped with by motor-driven cleaning element, to avoid insoluble slurry from being discharged from anaerobic fermentation reaction unit.
The present inventor is individually present some problems, limits them by studying and testing discovery, above-mentioned anaerobic device
Application.
For example, the anaerobic fermentation reaction unit provided with air floating structure, stirring scope is small, mixing effect is poor, influences COD processing
Effect, and the anaerobic fermentation reaction unit provided with flotation cell, are easily blocked, influence the stability of COD processing, also,
Above-mentioned air floating structure and flotation cell are both needed to be equipped with motor and agitating element or cleaning element, cause anaerobic fermentation reaction unit
It is complicated, cost is higher.
In addition, present inventor has further discovered that, for the waste water treatment process of cellulose ethanol, it is typically provided with height
Rate aeration process and dephosphorization process, and in the Waste Water Treatment of existing cellulose ethanol, high load capacity aeration process
Separately carried out with dephosphorization process, high load capacity aeration process and dephosphorization process are respectively necessary for being equipped with single equipment, so as to cause work
Sequence is cumbersome, and system forms complexity, and cost is higher.
In addition, with the development of industrial and agricultural production and the raising of living standards of the people, the discharge capacity of nitrogen and phosphorus pollutantses sharply increases.
Body eutrophication caused by nitrogen and phosphorus pollution is extremely serious, and lake " wawter bloom " and coastal waters " red tide " happens occasionally, and more drills more
It is strong.Body eutrophication has endangered all conglomeraties such as agricultural, fishery, tourist industry, and also drinking water hygiene and food security are formed
Huge threat.Cost-effective control nitrogen and phosphorus pollution has turned into current great environmental protection subject anxious to be resolved.Guanite,
Molecular formula is MgNH4PO46H2O, is a kind of white crystal for being insoluble in water, and under normal temperature, the solubility product in water is 2.5
×10-13.By adding chemical reagent, the ammonia in waste water and phosphate can be made to form guanite, realized to nitrogen and phosphorus pollutantses
Remove simultaneously.In addition, guanite contains two kinds of nutrients of nitrogen phosphorus, it is a kind of good slow-release fertilizer.
Guanite solubility in water and alkali is very low, and the ammonia nitrogen and phosphate in waste water are removed using the method for forming guanite,
The characteristics of with high-efficient simple.As wastewater from starch industry, livestock breeding wastewater, percolate from garbage filling field etc. are containing highly concentrated
The ammonia nitrogen of degree, it is difficult to directly carry out biological treatment, it usually needs handled in advance using physico-chemical process (such as blow-off method).Stripping
Method requires that pH is up to more than 10, and inefficient (being no more than 50%), easily causes secondary pollution.If with the guanite precipitation method
Processing, the requirement to pH conditions reduce than blow-off method, and efficiency is also higher.The examination made according to T ü nay et al. to leather-making waste water
Test, under conditions of pH is 8~9, using guanite dephosphorization method NH4+ clearances can be made to be up to more than 75%.Li et al. is adopted
With the guanite precipitation method, percolate of the initial ammonia nitrogen concentration in 5618mg/l was down to 210mg/l in 15 minutes, removed
Rate is more than 96%.And pH then need to be only controlled between 8.5 to 9.Chimenos et al. is 2320 to NH4+-N initial concentrations
In the experiment of mg/l waste water from dyestuff, NH4+-N clearances have also reached more than 90%.
On the one hand phosphorus is again on the one hand most valuable mineral resources as the key factor for causing eutrophication.In the world
The phosphorus storage level verified is only sufficient to the mankind and used 100 years.Because guanite can be directly as fertilizer, therefore it is considered as most to have
One of phosphorus recovery approach of prospect, Second phosphorus recovery International Academic Conference is also this ad hoc special topic, is carried out relevant from sewage
Reclaim the research of phosphorus.NH4+-N and PO43--P containing higher concentration in anaerobic digester effluent, it is adapted to use birds droppings
The stone precipitation method are handled.As long as a small amount of Mg2+ of addition, you can so that the solubility product of the various ions in waste water reaches satiety
And state, form guanite precipitation.And because its SS is relatively low, the guanite purity of production is higher.Mg (OH) 2 and NaOH
Sludge-digestion liquid is put into 1: 1 molar ratio relation, to increase pH, guanite is precipitated with fine granularity in fluid bed.
Phosphorus recovery device can realize 90% soluble phosphate recovery at present, ensure biological phosphate-eliminating operation up to standard.At actual waste water
In reason, there is a variety of limiting factors for the guanite precipitation method.First, the concentration of nitrogen and phosphorus in many waste water is very high, but each other it
Between ratio can not meet the requirements of the guanite precipitation method.In this case, deposition efficiency can be improved by adding some ions,
But processing cost can be increased.And nitrogen phosphorus is the control targe of wastewater treatment in itself, excessive addition can cause secondary pollution.Cross
The Mg2+ of amount addition is necessary for the guanite precipitation method, and therefore, cheap additive is that can the guanite precipitation method
The key of practical application.Mg (OH) 2 is more satisfactory Mg2+ additives, has both increased Mg2+ contents, can improve pH again.
The mud of Mg (OH) 2 uses in actual production.
In actual waste water processing, often except containing nitrogen and phosphorus pollution beyond the region of objective existence, can also contain organic pollution in waste water, if
These pollutants are not added with removing, and after guanite technique is taken, meeting entrainment portions organic pollution in guanite, reduce birds droppings
The purity and value of stone, in turn result in secondary pollution.
In summary, for actual waste water, the reaction dress of organic pollution, nitrogen and phosphorus that exploitation can be gone in water removal simultaneously
Put, will have great importance.Under the guiding of this thinking, present inventor proposes a kind of dephosphorization reaction unit,
For removing ammonia nitrogen (NH4+), phosphate (PO43-) and COD simultaneously from waste water, while sewage is handled, may be used also
To reclaim guanite as phosphate fertilizer.
In view of the cellulose alcohol wastewater treatment technology situation in correlation technique, the present invention propose it is a kind of it is simple in construction,
Cost is low, the Waste Water Treatment 1 of the cellulose ethanol of COD and nitrogen phosphorus high treating effect.
Below with reference to the accompanying drawings the Waste Water Treatment 1 of cellulose ethanol according to embodiments of the present invention is described.
As Figure 1-Figure 11, the Waste Water Treatment 1 of cellulose ethanol according to embodiments of the present invention includes anaerobic fermentation
Reaction unit 10, waste water dephosphorization reaction unit 20, denitrification reactor 40 and advanced treatment system 60.
Anaerobic fermentation reaction unit 10, waste water dephosphorization reaction unit 20, denitrification reactor 40 and advanced treatment system 60 are along useless
Water treatment technology direction is sequentially connected.
Wherein, anaerobic fermentation reaction unit 10 includes anaerobic fermentation tank body 100, stripping tube 200 and air supply pipe 300.Anaerobism
There is anaerobic reaction room 110, anaerobic reaction room 110 has waste water inlet 111, delivery port 112 and row in fermentation tank 100
Gas port 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 gas
Carrying the lower end of pipe 200 has air inlet 211.Air supply pipe 300 is connected with the air inlet 211 of stripping tube 200, for gas
Carry the gas supplied in pipe 200 for air lift.The gas for being used for air lift can be oxygen-depleted gas or inert gas, be preferably
Biogas.
Waste water dephosphorization reaction unit 20 includes dephosphorization reacting tank body 1100, aerator 1200 and degassing precipitation separator 1300.
There is dephosphorization reative cell 1110 in dephosphorization reacting tank body 1100, dephosphorization reative cell 1110 has water inlet 1111 and dephosphorization agent
Adding mouth 1112.Aerator 1200 is located in dephosphorization reative cell 1110.It is anti-that degassing precipitation separator 1300 is located at dephosphorization
Answer in room 1110, and the precipitation separator 1300 that deaerates is located at the top of aerator 1200, degassing precipitation separator 1300 is used
In separation gas and water and sludge.
It will be appreciated by those skilled in the art that ground is, waste water treatment process direction refers to, in whole processes of wastewater treatment,
Along the ordering of each operation, flow direction of the waste water from the first procedure sequentially into last procedure, i.e., along " anaerobism is sent out
The direction of 40 → advanced treatment system of ferment reaction unit 10 → waste water dephosphorization, 20 → denitrification reactor of reaction unit 60 ".
Below with reference to the accompanying drawings the wastewater treatment mistake of the Waste Water Treatment 1 of cellulose ethanol according to embodiments of the present invention is described
Journey.
Waste water enters anaerobic reaction room 110 by waste water inlet 111, and air supply pipe 300 supplies to stripping tube 200, anaerobic reaction room
Anaerobic environment is formed in 110, meanwhile, stripping tube 200 is played and stirred by exporting lift gas into anaerobic reaction room 110
Mix the effect of waste water and anaerobic sludge, thus, the waste water in anaerobic reaction room 110 mixes rapidly with anaerobic sludge, waste water with
The intense contact of anaerobic sludge makes the organic pollutant degradation in waste water, and unnecessary gas is by exhaust outlet in anaerobic reaction room 110
113 discharges, the waste water after anaerobic fermentation purifies flow out anaerobic reaction room 110 by delivery port 112, and by water inlet 1111
Into dephosphorization reative cell 1110, dephosphorization agent (such as oxygen is added into dephosphorization reative cell 1110 by dephosphorization agent adding mouth 1112
Change magnesium), aerator 1200 supplies oxygen aeration into dephosphorization reative cell 1110, and aerobic environment is formed in dephosphorization reative cell 1110,
Meanwhile aerator 1200 supply air play a part of stir waste water, thus the waste water in dephosphorization reative cell 1110 with
Aerobic sludge and dephosphorization agent mix rapidly, remove the biochemical organic matter of deliquescent colloidal state in waste water and carry out dephosphorization,
Waste water outflow after reacted is precipitated in separator 1300 to degassing, thus gas, water and aerobic sludge separation, after separation
Gas is discharged by the top of dephosphorization reative cell 1110, and then, water separates with aerobic sludge, and the aerobic sludge after separation is from degassing
Precipitate separator 1300 and return to recycling in dephosphorization reative cell 1110, it is heavy that the water overflow after being separated with aerobic sludge goes out degassing
Shallow lake separator 1300, discharge dephosphorization reative cell 1110, it is delivered to denitrification reactor 40 and carries out denitrogenation, the waste water after denitrogenation enters
Enter advanced treatment system 60, can not biodegradable organic pollution in waste water further to remove.
The Waste Water Treatment 1 of cellulose ethanol according to embodiments of the present invention, by set along waste water treatment process direction according to
Anaerobic fermentation reaction unit 10, waste water dephosphorization reaction unit 20, denitrification reactor 40 and the advanced treatment system 60 of secondary connection,
Can be by the COD processing in cellulose alcohol wastewater to below 100mg/L.
Also, by setting stripping tube 200 and air supply pipe 300 in anaerobic fermentation reaction unit 10, air supply pipe can be utilized
300 provide gas into stripping tube 200, and can the output gas progress into anaerobic reaction room 110 using stripping tube 200
Air lift, 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
Effect.On the other hand, by setting stripping tube 200, can cancel motor that air floating structure and air floating structure need to be equipped with and
Agitating element, the structure of anaerobic fermentation reaction unit 10 is simplified, reduce the cost of anaerobic fermentation reaction unit 10.Separately
Outside, anaerobic fermentation reaction unit 10 according to embodiments of the present invention eliminates motor that flotation cell and flotation cell need to be equipped with and clear
Clean element, further simplify the structure of anaerobic fermentation reaction unit 10, and reduce further anaerobic fermentation reaction unit
10 cost.
In addition, by setting dephosphorization agent adding mouth 1112 on dephosphorization reacting tank body 1100, and in dephosphorization reative cell 1110
Aerator 1200 is set, aeration and phosphorus removal functional are integrated with, it is possible thereby to instead of in cellulose alcohol wastewater processing system
High load capacity is aerated process and dephosphorization process each required equipment, so as to the structure of simplification cellulose alcohol wastewater processing system,
Reduce the cost of cellulose alcohol wastewater processing system, and COD high treating effects.
The Waste Water Treatment 1 of cellulose ethanol according to embodiments of the present invention, have it is simple in construction, cost is low, at COD
Manage the advantages that effect is good.
Below with reference to the accompanying drawings the Waste Water Treatment 1 of cellulose ethanol according to the specific embodiment of the invention is described.
As Figure 1-Figure 11, the Waste Water Treatment 1 of cellulose ethanol according to embodiments of the present invention is included along waste water
Anaerobic fermentation reaction unit 10, waste water dephosphorization reaction unit 20, denitrification reactor 40 and the depth that reason direction is sequentially connected
Reason system 60.
Advantageously, as shown in Fig. 2, Fig. 6, Fig. 9 and Figure 11, the lower end of stripping tube 200 is adjacent to anaerobic reaction room 110
Bottom, and the upper end of stripping tube 200 extends to the top of anaerobic reaction room 110, delivery port 112 is located at anaerobic reaction room 110
Top and higher than stripping tube 200 upper end.The gas that air supply pipe 300 provides is by stripping tube 200, by anaerobic reaction room
110 bottom is transported to the top of anaerobic reaction room 110, and is exported from gas outlet 221 with anaerobic reaction room 110
Waste water and anaerobic sludge mixture be stirred, thus, can not only be provided in order to air supply pipe 300 into stripping tube 200
Gas, and the stirring scope and mixing effect of stripping tube 200 can be further improved, and the gas exported by stripping tube 200
Water outlet of the body without interference with delivery port 112.
Alternatively, as shown in Fig. 2, Fig. 6, Fig. 9 and Figure 11, the upper surface of stripping tube 200 is opened wide to form gas outlet 221,
The lower surface of stripping tube 200 is opened wide to form air inlet 211, can so increase air inlet 211 and outlet to greatest extent
The valid circulation area of mouth 221, 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 Fig. 2, Fig. 6, Fig. 9 and Figure 11, stripping tube 200 wraps
Include straight length 210 and segmental arc 220.Straight length 210 vertically extends, and segmental arc 220 is upper with straight length 210
End is connected, and the angle α between the opening direction and vertically downward direction of gas outlet 221 is more than or equal to zero degree and less than 180
Degree, i.e. 180 ° of 0 °≤α ＜.
Preferably, as shown in Fig. 6 and Figure 11, segmental arc 220 to be inverted U-shaped, the opening direction of gas outlet 221 straight down,
In other words, α=0 °.So by the gas that stripping tube 200 exports from the top of anaerobic reaction room 110 stir downwards waste water and
The mixture of anaerobic sludge, stirring scope and mixing effect are further increased, so as to further improve anaerobic fermentation reaction dress
Put 10 COD treatment effects.
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 level
It is arranged at intervals in face 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. 6, anaerobic fermentation reaction unit 10 also includes precipitation separator 400,
Precipitation separator 400 is located in anaerobic reaction room 110 and had positioned at the top of stripping tube 200, precipitation separator 400 with going out
The connected separator delivery port 413 in the mouth of a river 112, the phase of water inlet 1111 of delivery port 112 and waste water dephosphorization reaction unit 20
Even.Waste water outflow after anaerobic fermentation purifies is to precipitating in separator 400, and thus gas separates with water and anaerobic sludge,
Gas after separation is discharged by exhaust outlet 113, and then, water separates with anaerobic sludge, and the anaerobic sludge after separation divides from precipitation
Return in anaerobic reaction room 110 and recycle from device 400, the separator delivery port 413 after separation is transported to delivery port
112, discharge anaerobic reaction room 110 is simultaneously delivered to waste water dephosphorization reaction unit 20.
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 fig. 7, precipitation separator 400 includes casing 410, dividing plate 420, precipitation inclined plate 430 and overflow
Flow weir 440.
Chamber 411 is precipitated formed with deaerating in casing 410, the bottom of degassing precipitation chamber 411 has sludge outlet 412, and degassing is sunk
The cross-sectional area of the bottom of shallow lake chamber 411 is gradually reduced along direction from the top down.Dividing plate 420 is located at degassing precipitation chamber 411
The top for the precipitation chamber 411 that deaerates is separated into degassing district 421 and settling zone 422 by top, dividing plate 420, degassing district 421
Bottom is connected with the bottom of settling zone 422 so that waste water overflows in degassing district 421 from anaerobic reaction room 110 and then from degassing
The bottom in area 421 is flowed in settling zone 422.Precipitation inclined plate 430 is located in settling zone 422.Downflow weir 440 is located at precipitation
In area 422 and downflow 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. 7.
Gas-entrained and anaerobic sludge in water after anaerobic sludge is degraded, the gas-entrained and water overflow of anaerobic sludge to degassing
The degassing district 421 of chamber 411 is precipitated, wherein gas is escaped from degassing district 421, discharged by exhaust outlet 113, completes 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, and now anaerobism is dirty
Mud 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 sludge outlet 412
Discharge precipitation separator 400 enters anaerobic reaction room 110, continues on for wastewater degradation, with detesting in degassing precipitation chamber 411
In water overflow to the overflow launder 441 of downflow weir 440 after the separation of oxygen sludge, and successively by separator delivery port 413 and water outlet
Mouth 112 discharges anaerobic reaction rooms 110, carries out subsequent treatment.During anaerobic sludge rises with water, anaerobic sludge is precipitating
Settled on swash plate 430 and be slipped to degassing precipitation chamber 411 bottom, contribute to anaerobic sludge to be separated from water, so far, completion water,
The separation of anaerobic sludge and gas.
Advantageously, as shown in fig. 7, the upper edge that the casing 410 of degassing district 421 is limited with dividing plate 420 is less than dividing plate 420
Upper edge and limited with dividing plate 420 settling zone 422 the part of casing 410 upper edge.In other words, the limit of casing 410
Make the upper edge of the part of degassing district 421, less than edge on the part for limiting settling zone 422 of casing 410, and less than every
The upper edge of plate 420.On downflow weir 440 along can with the part for limiting degassing district 421 of casing 410 along concordant
Or the upper edge of the part for limiting degassing district 421 higher than casing 410, and the upper edge of downflow weir 440 is less than casing 410
The part for limiting settling zone 422 on along and dividing plate 420 upper edge.Thus it can be prevented that water in degassing district 421 from
Top overflow ensures that the water in degassing district 421 flow to settling zone 422 from the bottom of degassing district 421, and then make to settling zone 422
Anaerobic sludge is sufficiently separated, and the water in settling zone 422 is by overflow to overflow launder 441, avoiding overflow launder 441
Anaerobic sludge is carried secretly in interior water.
Alternatively, as shown in fig. 7, casing 410 is cuboid, the lower end of the first longitudinal side wall 414 of the bottom of casing 410
Extend downward beyond the lower end of the second longitudinal side wall 415 of the bottom of casing 410, and the lower end and second of the first longitudinal side wall 414
The lower end of longitudinal side wall 415 is overlapping in the vertical direction.It is possible thereby to advantageously avoid the anaerobic sludge in anaerobic reaction room 110
The degassing for entering precipitation separator 400 by sludge outlet 412 is precipitated in chamber 411.
For example, in four longitudinal side walls of casing 410, two longer longitudinal side walls of length are respectively first in the horizontal direction
The lower end of the longitudinal side wall 415 of longitudinal side wall 414 and second, the lower end of the first longitudinal side wall 414 and the second longitudinal side wall 415 is relative to
The upper end of one 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 second
The lower section of the lower end of longitudinal side wall 415, and the lower end of the first longitudinal side wall 414 and the lower end of the second longitudinal side wall 415 are in the horizontal plane
Projection it is 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,
Thus can smoothly be returned by sludge outlet 412 after on the one hand can ensureing the anaerobic sludge precipitation in degassing precipitation chamber 411
Anaerobic reaction room 110, and on the other hand the structure of the sludge outlet 412 can stop that the anaerobism in anaerobic reaction room 110 is dirty
Mud enters degassing precipitation chamber 411 from sludge outlet 412, ensures the anaerobic sludge separating effect of precipitation separator 400.
In some specific embodiments of the present invention, as shown in figures 9 and 11, it is heavy that anaerobic fermentation reaction unit 10 also includes
Shallow lake separator 400, precipitation separator 400 are located at outside anaerobic fermentation tank body 100, and delivery port 112 is by precipitating separator 400
It is connected with the water inlet 1111 of waste water dephosphorization reaction unit 20.Precipitating separator 400 includes casing 410, precipitation inclined plate 430
With downflow weir 440.
Degassing precipitation chamber 411 is formed in casing 410, degassing precipitation chamber 411 has import 416, the and of separator delivery port 413
Sludge outlet 412, import 416 connect with the delivery port 112 of anaerobic reaction room 110, separator delivery port 413 and waste water
The water inlet 1111 of dephosphorization reaction unit 20 is connected, and at least one conical cavity is formed at the bottom of degassing precipitation chamber 411, each
The cross-sectional area of conical cavity is gradually reduced along direction from the top down, and sludge outlet 412 is formed in the bottom of the conical cavity.
Precipitation inclined plate 430 is located in degassing precipitation chamber 411.Downflow weir 440 is located in degassing precipitation chamber 411, and downflow weir 440
It is interior formed with the downflow weir 440 connected with separator delivery port 413.
Below with reference to separation process of Fig. 9 and Figure 11 description precipitation separators 400 to water, gas and anaerobic sludge.
Gas-entrained and anaerobic sludge in the water flowed out by the delivery port 112 of anaerobic reaction room 110, gas-entrained and anaerobism are dirty
The water of mud enters degassing precipitation chamber 411 by import 416, and wherein gas escapes from ullage and discharges degassing precipitation chamber 411,
Complete gas separation.Water entrainment anaerobic sludge after being separated with gas, wherein anaerobic sludge precipitation are sunk and precipitate chamber in degassing
To sludge outlet 412 under the guiding of the inwall of 411 lower taper chambers, degassing precipitation chamber 411 is discharged by sludge outlet 412,
In water overflow to the overflow launder 441 of downflow weir 440 after being separated in degassing precipitation chamber 411 with anaerobic sludge, and by separator
The discharge degassing precipitation chamber 411 of delivery port 413, carries out subsequent treatment.During anaerobic sludge rises with water, anaerobic sludge exists
Settled on precipitation inclined plate 430 and be slipped to the conical cavity of degassing precipitation chamber 411 bottom, contribute to anaerobic sludge to be separated from water,
So far, the separation of water, anaerobic sludge and gas is completed.
Thus, it is possible to gas, water and anaerobic sludge are first isolated using precipitating separator 400 outside anaerobic reaction room 110,
Product after separation is each delivered to different regions again, improves the pure of water outlet.
Further, as shown in figures 9 and 11, anaerobic fermentation reaction unit 10 also includes sinker 500,
Sinker 500 is connected between the import 416 of delivery port 112 and degassing precipitation chamber 411 of anaerobic reaction room 110.So
Sinker 500 can be utilized to consume and disperse the energy of the water flowed out by anaerobic fermentation tank body 100, prevent or mitigate by anaerobism
Erosion damage of the water that fermentation tank 100 flows out to precipitation separator 400.
Advantageously, as shown in figures 9 and 11, anaerobic fermentation reaction unit 10 also includes mud return line 600, sludge reflux
One end of pipe 600 connects with anaerobic reaction room 110, and the sludge outlet 412 of degassing precipitation chamber 411 passes through sludge discharge pipe 700
It is connected with mud return line 600, mud return line 600 is provided with sludge reflux pump 610, is discharged from sludge outlet 412
Anaerobic sludge can pass sequentially through sludge discharge pipe 700 and mud return line 800 returns to anaerobic reaction room 110, so as to carry out
Recycle.
Alternatively, for external precipitation separator 400, hydrocyclone or external air-floating apparatus can be used to replace.
In some specific examples of the present invention, as shown in figure 11, the bottom of anaerobic reaction room 110 has mud discharging mouth 115,
Mud discharging mouth 115 is connected with mud discharging valve and/or mud discharging pump 116, and unnecessary anaerobism is dirty in anaerobic reaction room 110
Mud can discharge anaerobic reaction room 110 by mud discharging mouth 115.
Alternatively, as shown in figures 9 and 11, waste water inlet 111 is connected with charging pump 117, anti-to anaerobism to control whether
Answer the transport wastewater of room 110 and the wastewater flow rate conveyed to anaerobic reaction room 110.As depicted in figs. 1 and 2, air supply pipe 300
The gas control valve 118 outside the anaerobic reaction room 110 is provided with, to control whether to supply to stripping tube 200 and to gas
Put forward the air demand of pipe 200.
Further, the water inlet pipe at waste water inlet 111 can be connected with water-locator, or water distributing pore is opened up on water inlet pipe.
Advantageously, as shown in Fig. 2, Fig. 6, Fig. 9 and Figure 11, anaerobic fermentation reaction unit 10 also includes water sealed tank 800,
The top of anaerobic fermentation tank body 100 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 using water sealed tank 800, maintain the pressure of anaerobic reaction room 110, and back-fire relief effect can be played, additionally may be used
To play certain clean-up effect to biogas.
Alternatively it is also possible to water sealed tank 800 is replaced using safety valve.
In some specific embodiments of the present invention, as shown in figure 3, waste water dephosphorization reaction unit 20 also includes aeration pump or exposure
Gas blower fan 1700, aeration pump or Aeration fan 1700 be located at the outside of dephosphorization reacting tank body 1100 and with the phase of aerator 1200
Even, with to the pumped air of aerator 1200.In certain embodiments, aerator 1200 is for blast aeration and including exposing
Gas airduct and the aeration plate or aeration tube installed in aeration airduct end, aeration pump or Aeration fan 1700 will by being aerated airduct
Air is transported to aeration tube or aeration plate, and aeration tube or aeration plate are by air aeration to dephosphorization reative cell 1110.
Alternatively, aerator 1200 can be jetting type aerator, in the case, without being located at dephosphorization reacting tank body
The aeration pump or Aeration fan 1700 of 1100 outsides, jetting type aerator utilize jetting type hydraulic blow formula air-diffuser
Draw air into dephosphorization reative cell 1110, such as the ejector being located in dephosphorization reative cell 1110 is anti-with reference to dephosphorization is located at
Answer the jet pump outside tank body 1100.
Advantageously, as shown in figure 3, water inlet 1111 is connected with the waste water control valve 1114 outside dephosphorization reacting tank body 1100,
To control whether the wastewater flow rate conveyed to the transport wastewater of dephosphorization reative cell 1110 and to dephosphorization reative cell 1110.
As shown in figure 3, smoothly put into dephosphorization reative cell 1110 for convenience of dephosphorization agent and avoid other impurity etc. anti-into dephosphorization
Room 1110 to be answered, while plays insulation and reduces the effect of heating energy consumption, the top of dephosphorization reacting tank body 1100 is provided with top cover 1115,
Dephosphorization agent adding mouth 1112 is located on top cover 1115.
In some specific embodiments of the present invention, as shown in figure 3, aerator 1200 has multiple aeration heads or aeration tube
1210, multiple aeration heads or aeration tube 1210 are arranged at intervals in dephosphorization reative cell 1110, and aerator 1200 is by multiple
Aeration head or aeration tube 1210 improve the even results of oxygen supply and waste water are become reconciled to the uniform aeration of dephosphorization reative cell 1110
The uniform stirring effect of oxygen sludge.
Further, as shown in figure 3, waste water dephosphorization reaction unit 20 also includes multiple guide shells 1400, guide shell 1400
Quantity it is corresponding with the quantity of aeration head or aeration tube 1210, the top and bottom of each guide shell 1400 are opened wide, multiple
Aeration head or aeration tube 1210 stretch into multiple guide shells 1400 from the lower end of multiple guide shells 1400 respectively.It is thus, it is possible to sharp
Guide functions are played with multiple guide shells 1400, so as to further make the waste water in dephosphorization reative cell 1110 and aerobic dirt
Mud fully contacts, and aerobic sludge is in suspended state, the exposure level of waste water and aerobic sludge is improved, so as to improve wastewater treatment
Efficiency.
With reference to the design of guide shell, Mg (OH) 2 emulsion is added under optimum reaction condition, generates ammonia magnesium phosphate
(MgNH4PO4.6H2O, being commonly called as guanite) crystallizes.Under such circumstances, a part of COD can also be by waste water
Dissolved oxygen is removed, and forms new biomass and carbon dioxide.
Alternatively, as shown in figure 3, waste water dephosphorization reaction unit 20 also includes water-locator 1500, water-locator 1500, which is located at, to be removed
In phosphorus reaction room 1110 and positioned at the lower section of aerator 1200, water-locator 1500 is connected with water inlet 1111, and water-locator
1500 with the multiple water distribution mouths 1510 being arranged at intervals and Open Side Down.Waste water enters water-locator 1500 by water inlet 1111,
It is and dispersed in dephosphorization reative cell 1110 by multiple water distribution mouths 1510 of water-locator 1500.
In some specific examples of the present invention, as shown in figure 3, waste water dephosphorization reaction unit 20 also includes cyclone 1600,
Dephosphorization reative cell 1110 has the discharge gate 1113 positioned at the bottom of dephosphorization reacting tank body 1100, and cyclone 1600 has eddy flow
Device import 1610, mud mouth 1620 and cyclone outlet 1630, cyclone inlets 1610 are connected and revolved with discharge gate 1113
Blow-off valve 1116 is connected between stream device import 1610 and discharge gate 1113, cyclone outlet 1630 passes through return pipe 1640
It is connected with dephosphorization reative cell 1110.
Discharge gate 1113, blow-off valve 1116 and rotation can be passed through successively by being deposited on the liquid-solid mixture of the bottom of dephosphorization reative cell 1110
Stream device import 1610 enters cyclone 1600 and separated in cyclone 1600, and the water after separation passes sequentially through cyclone
Outlet 1630 and return pipe 1640 return to dephosphorization reative cell 1110, and the solid (such as ammonium magnesium phosphate) after separating is by mud mouth
1620 are delivered to birds droppings pond, can be used as fertilizer.
With reference to the design of cyclone, to separate struvite crystals and activated sludge and water, to improve the purity of guanite simultaneously
As fertilizer application.
Compared to traditional dephosphorization apparatus, such as compared with the device for adding molysite, the dephosphorization reaction unit cost of the embodiment of the present invention
Lower, the multiple purposes of set of device (except ammonia nitrogen and COD), caused guanite does not cause secondary pollution not only, or slow
Release N, P, Mg fertilizer.Guanite particle is separated by cyclone from device, and its quality meets such as European Union
Fertilizer relevant criterion.
In some specific embodiments of the present invention, waste water dephosphorization reaction unit 20 also includes pump and the desliming device being connected with pump,
Clear liquid after the desliming device removing sludge, which returns to, states dephosphorization reative cell 1110, so as to improve the utilization rate of waste water.
Alternatively, the desliming device can use settler replace, i.e., waste water dephosphorization reaction unit 20 also include pump and with
The connected settler of the pump, the stillness of night after the settler precipitates return to dephosphorization reative cell 1110.
In some specific examples of the present invention, as shown in Figure 3 and Figure 4,.Degassing precipitation separator 1300 includes separator
Body 1310, baffle plate 1320, inclined settling plate tilt sediment tube 1330 and effluent overflow weir water 1340.
Formed with degassing mud chamber 1311, the bottom of degassing mud chamber 1311 there is sludge to arrange mouth in separator body 1310
1314, the cross-sectional area of the bottom for the mud chamber 1311 that deaerates is gradually reduced along direction from the top down.Baffle plate 1320 is located at de-
The top for the mud chamber 1311 that deaerates is separated into devolatilizing chamber 1312 and precipitation chamber by the top of gas mud chamber 1311, baffle plate 1320
1313, the bottom of devolatilizing chamber 1312 with precipitate the bottom of chamber 1313 connect so as to waste water overflow to from dephosphorization reative cell 1110 it is de-
Flowed in air cavity 1312 and then from the bottom of devolatilizing chamber 1312 in precipitation chamber 1313.Inclined settling plate tilts sediment tube 1330
It is located in precipitation chamber 1313.Effluent overflow weir water 1340 be located at precipitation chamber 1313 in and effluent overflow weir water 1340 formed have with
The water outlet overflow launder 1341 for the separation outlet 1342 that denitrification reactor 40 connects.
Below with reference to separation process of Fig. 3 and Fig. 4 description degassing precipitation separators 1300 to water, gas and aerobic sludge.
Gas-entrained and aerobic sludge in water after aerobic sludge is degraded, the gas-entrained and water overflow of aerobic sludge to degassing
The devolatilizing chamber 1312 of mud chamber 1311, wherein gas escape from devolatilizing chamber 1312, are arranged by the top of dephosphorization reative cell 1110
Go out, complete gas separation.The water of entrainment aerobic sludge after being separated with gas precipitates chamber by the bottom flow direction of devolatilizing chamber 1312
1313, arrange mouth to sludge under now aerobic sludge precipitation sinking and the guiding of the inwall in the degassing lower tilt of mud chamber 1311
1314, degassing precipitation separator 1300 is discharged by sludge row's mouth 1314 and enters dephosphorization reative cell 1110, continues on for waste water drop
Solve, the water outlet overflow launder 1341 of the water overflow after being separated in degassing mud chamber 1311 with aerobic sludge to effluent overflow weir water 1340
It is interior, and be expelled to by separation outlet 1342 outside dephosphorization reative cell 1110, carry out subsequent treatment.Aerobic sludge rose with water
Cheng Zhong, aerobic sludge settle on inclined settling plate or inclination sediment tube 1330 and are slipped to the degassing bottom of mud chamber 1311,
Contribute to aerobic sludge to be separated from water, so far, complete the separation of water, aerobic sludge and gas.
Advantageously, as shown in figure 4, the upper edge that the separator body 1310 of devolatilizing chamber 1312 is limited with baffle plate 1320 is less than
The upper edge of baffle plate 1320 and the upper edge that the part of separator body 1310 for precipitating chamber 1313 is limited with baffle plate 1320.Change
Yan Zhi, the upper edge of the part for limiting devolatilizing chamber 1312 of separator body 1310, less than the restriction of separator body 1310
Go out to precipitate edge on the part of chamber 1313, and less than the upper edge of baffle plate 1320.Along can be with separating on effluent overflow weir water 1340
Along concordant or higher than separator body 1310 limit degassing on the part for limiting devolatilizing chamber 1312 of device body 1310
The upper edge of the part of chamber 1312, and the upper edge of effluent overflow weir water 1340 limits precipitation chamber less than separator body 1310
Edge and the upper edge of baffle plate 1320 on 1313 part.It thus it can be prevented that water in devolatilizing chamber 1312 from top overflow to heavy
Shallow lake chamber 1313, ensure that the water in devolatilizing chamber 1312 flow to precipitation chamber 1313 from the bottom of devolatilizing chamber 1312, and then make aerobic sludge
It is sufficiently separated, and precipitates the water in chamber 1313 by overflow to water outlet overflow launder 1341, avoiding water outlet overflow launder 1341
Aerobic sludge is carried secretly in interior water.
Alternatively, as shown in figure 4, the cross section of separator body 1310 is rectangle, for example, cuboid, separator body
The lower end of first longitudinal side wall 1315 of 1310 bottom extends downward beyond the second longitudinal side wall of the bottom of separator body 1310
1316 lower end, and the lower end of the first longitudinal side wall 1315 is overlapping in the vertical direction with the lower end of the second longitudinal side wall 1316.By
This can advantageously be avoided the aerobic sludge in dephosphorization reative cell 1110 from arranging mouth 1314 into degassing precipitation separator by sludge
In 1300 degassing mud chamber 1311.
For example, in four longitudinal side walls of separator body 1310, two longer longitudinal side walls of length are distinguished in the horizontal direction
For the first longitudinal side wall 1315 and the second longitudinal side wall 1316, under the lower end of the first longitudinal side wall 1315 and the second longitudinal side wall 1316
End is mutually adjacent relative to the upper end of the first longitudinal side wall 1315 and the upper end of the second longitudinal side wall 1316, the first longitudinal side wall 1315
Lower end is located at the lower section of the lower end of the second longitudinal side wall 1316, and the lower end of the first longitudinal side wall 1315 and the second longitudinal side wall 1316
The projection of lower end in the horizontal plane is overlapping, between the lower end of the lower end of the first longitudinal side wall 1315 and the second longitudinal side wall 1316 between
Gap forms sludge row's mouth 1314, can after the aerobic sludge precipitation that thus on the one hand can ensure to deaerate in mud chamber 1311
Mouth 1314 is arranged by sludge and smoothly returns to dephosphorization reative cell 1110, and on the other hand the structure of sludge row mouth 1314 can hinder
The aerobic sludge kept off in dephosphorization reative cell 1110 enters degassing mud chamber 1311 from sludge row's mouth 1314, ensures degassing precipitation point
From the aerobic sludge separating effect of device 1300.
In some specific embodiments of the present invention, as shown in Fig. 1, Fig. 5, Fig. 8 and Figure 10, denitrification reactor 40 includes
The anaerobic ammonia oxidation reactor 2100 and Anoxic/Aerobic reaction tank 2200 being sequentially connected along waste water treatment process direction.Wherein,
Anaerobic ammonia oxidation reactor 2100 is connected with waste water dephosphorization reaction unit 20, Anoxic/Aerobic reaction tank 2200 and advanced treating system
System 60 is connected, and the waste water flowed out by waste water dephosphorization reaction unit 20 flows through anaerobic ammonia oxidation reactor 2100 successively and anoxic is good
Oxygen reaction tank 2200 carries out denitrogenation processing.
In some specific examples of the present invention, the Waste Water Treatment 1 of cellulose ethanol also includes coagulation reaction device,
The coagulation reaction device is connected between denitrification reactor 40 and advanced treatment system 60, and the coagulation reaction device has
Coagulating basin, flocculation basin and the sedimentation basin being sequentially communicated along the waste water treatment process direction, dosing coagulant in coagulating basin, wadding
Flocculant is added in solidifying pond, sedimentation basin is used for the precipitation separation that deaerates.
In some specific embodiments of the present invention, as shown in Fig. 1, Fig. 5, Fig. 8 and Figure 10, advanced treatment system 60 wraps
Include the multigroup Fenton's reaction device 4100 being sequentially connected along the waste water treatment process direction, every group of Fenton's reaction device 4100
Including Fenton's reaction pond and Fenton sedimentation basin.The waste water flowed out by denitrification reactor 40 passes through every group of Fenton's reaction device 4100
Fenton's reaction pond and Fenton sedimentation basin, carry out Fenton oxidation, with further remove in waste water can not be biodegradable organic
Pollutant.
Specifically, as shown in Fig. 1, Fig. 5, Fig. 8 and Figure 10, have in each Fenton's reaction pond along the waste water
Multiple Fenton's reaction chambers 4111 and Fenton the flocculation chamber 4112 that handling process direction is sequentially communicated, each Fenton's reaction chamber 4111
Interior be provided with the fast mixer 4113 of Fenton and Fenton flocculation chamber 4112 is provided with the slow mixer 4114 of Fenton.Need exist for understanding ground
It is that the speed of the fast mixer 4113 of Fenton and the slow mixer 4114 of Fenton is the comparatively i.e. fast mixer 4113 of Fenton
Rotating speed is higher than the rotating speed of the slow mixer 4114 of Fenton.The He of Fenton tilted plate separator 4131 is provided with each Fenton sedimentation basin
Fenton mud scraper 4132.
For example, multiple Fenton's reaction ponds include one-level Fenton's reaction pond 4110 and two level Fenton's reaction pond 4120, more
The individual Fenton sedimentation basin includes one-level Fenton sedimentation basin 4130 and two level Fenton sedimentation basin 4140, one-level Fenton's reaction pond
4110th, one-level Fenton sedimentation basin 4130, two level Fenton's reaction pond 4120 and two level Fenton sedimentation basin 4140 are along at the waste water
Reason process orientation is sequentially connected.Wherein, in each in one-level Fenton's reaction pond 4110 and two level Fenton's reaction pond 4120
Three Fenton's reaction chambers 4111 being sequentially communicated along the waste water treatment process direction and a Fenton flocculation chamber 4112 are respectively provided with,
It is respectively equipped with three Fenton's reaction chambers 4111 in the fast mixer 4113 of Fenton and Fenton flocculation chamber 4112 and is stirred slowly provided with Fenton
Machine 4114.Fenton tilted plate separator 4131 is respectively equipped with one-level Fenton sedimentation basin 4130 and two level Fenton sedimentation basin 4140
With Fenton mud scraper 4132.
Further, as shown in Fig. 1, Fig. 5, Fig. 8 and Figure 10, advanced treatment system 60 also includes the He of sand filter 4200
Air reservoir 4300.Sand filter 4200 along the waste water treatment process direction with Fenton sedimentation basin (example last described
Such as two level Fenton sedimentation basin 4140) it is connected.Air reservoir 4300 is connected with sand filter 4200.By along the wastewater treatment work
The water of last Fenton sedimentation basin (such as two level Fenton sedimentation basin 4140) outflow on skill direction enters sand filter
4200, air reservoir 4300 is supplied to carry out filter sand to the water in sand filter 4200 to sand filter 4200, is improved by depth
The degree of purity for the water that reason system 60 flows out.
Alternatively, as shown in Fig. 1, Fig. 5, Fig. 8 and Figure 10, advanced treatment system 60 also includes sulfuric acid storage tank 4400, sulphur
Sour ferrous iron solution tank 4500, dioxygen water storage tank 4600 and Fenton flocculant tank 4700.
Sulfuric acid storage tank 4400 with multiple Fenton's reaction chambers 4111 in each Fenton's reaction pond along the wastewater treatment work
First on skill direction is connected, i.e. sulfuric acid storage tank 4400 and first Fenton's reaction chamber 4111 in one-level Fenton's reaction pond 4110
And first Fenton's reaction chamber 4111 in two level Fenton's reaction pond 4120 is connected, for providing sulfuric acid.Copperas solution
Tank 4500 with multiple Fenton's reaction chambers 4111 in each Fenton's reaction pond along the waste water treatment process direction
First is connected, i.e., first Fenton's reaction chamber 4111 in copperas solution tank 4500 and one-level Fenton's reaction pond 4110 with
And first Fenton's reaction chamber 4111 in two level Fenton's reaction pond 4120 is connected, for providing ferrous sulfate.Dioxygen water storage tank
4600 with multiple Fenton's reaction chambers 4111 in each Fenton's reaction pond along the on the waste water treatment process direction
One is connected, i.e. dioxygen water storage tank 4600 and first Fenton's reaction chamber 4111 and two level in one-level Fenton's reaction pond 4110
First Fenton's reaction chamber 4111 in Fenton's reaction pond 4120 is connected, for providing hydrogen peroxide.Fenton flocculant tank 4700 with
The Fenton flocculation chamber 4112 in each Fenton's reaction pond is connected, i.e. Fenton flocculant tank 4700 and one-level Fenton's reaction pond 4110
Fenton flocculation chamber 4112 and two level Fenton's reaction pond 4120 Fenton flocculation chamber 4112 be connected, for providing flocculant.
Below with reference to the accompanying drawings fibre according to embodiments of the present invention and with reference to the Waste Water Treatment 1 of above-mentioned cellulose ethanol is described
The method of wastewater treatment of dimension element ethanol processed, the method for wastewater treatment of cellulose ethanol according to embodiments of the present invention is including following
Step：
A：Waste water is delivered to anaerobic fermentation reaction unit 10, waste water carried out under anaerobic environment biodegradable.
B：The waste water flowed out by anaerobic fermentation reaction unit 10 is delivered to waste water dephosphorization reaction unit 20, it is anti-in waste water dephosphorization
Oxygen supply aeration in device 20 is answered, aerobic biodegradation and dephosphorization are carried out to the waste water after biodegradation.
C：The waste water flowed out by waste water dephosphorization reaction unit 20 is delivered to denitrification reactor 40, in denitrification reactor 40 to useless
Water carries out denitrogenation.
D：The waste water flowed out by denitrification reactor 40 is delivered to advanced treatment system 60, depths is carried out to the waste water after dephosphorization
Processing, so that further removal can not biodegradable organic pollution.
The method of wastewater treatment of cellulose ethanol according to embodiments of the present invention can simplied system structure, reduce cost, carry
High COD treatment effects.
The method of wastewater treatment of cellulose ethanol according to embodiments of the present invention, waste water is carried out successively anaerobic fermentation purification,
Dephosphorization, denitrogenation and advanced treating are aerated, can be excellent to below 100mg/L, COD treatment effects by the COD processing in waste water
Show, and the structure of the Waste Water Treatment of cellulose ethanol can be simplified, reduce the Waste Water Treatment of cellulose ethanol
Cost.
In some specific embodiments of the present invention, in the step A, it is passed through in anaerobic fermentation reaction unit 10 under
The compressed biogas of supreme flowing, so that waste water and sludge fully contact.
Further, in the step A, using the precipitation separator 400 of anaerobic fermentation reaction unit 10, biology is dropped
Waste water after solution is de-gassed precipitation separation, the step B is carried out to the waste water after degassed precipitation separation, to be removed into
Gas and solid before step B in waste water.
Alternatively, in the step B, it is passed through air to waste water dephosphorization reaction unit 20 and is aerated, and to waste water dephosphorization
Addition magnesia is as dephosphorization oxidant, such as magnesia in reaction unit 20.
In some specific examples of the present invention, the step C includes following sub-step：
C1：The waste water flowed out by waste water dephosphorization reaction unit 20 is delivered to the anaerobic ammonia oxidation reactor of denitrification reactor 40
2100, to carry out Anammox reaction to the waste water after aeration.
C2：The waste water flowed out by the anaerobic ammonia oxidation reactor 2100 of denitrification reactor 40 is delivered to denitrification reactor 40
The hypoxia response intracavitary of Anoxic/Aerobic reaction tank 2200, to enter under anaerobic environment to passing through the reacted waste water of Anammox
Row anti-nitration reaction.
C3：It is anti-that waste water by the hypoxia response intracavitary of the Anoxic/Aerobic reaction tank 2200 of denitrification reactor 40 is delivered to denitrogenation
The aerobic reaction intracavitary of the Anoxic/Aerobic reaction tank 2200 of device 40 is answered, to the waste water by anti-nitration reaction under aerobic environment
Carry out nitration reaction.
In some specific examples of the present invention, after the step C, coagulation first is carried out to the waste water after denitrogenation, then carry out
The step D.
In some specific embodiments of the present invention, the step D includes following sub-step：
D1：The waste water flowed out from denitrification reactor 40 is delivered to one-level Fenton's reaction pond 4110, to enter to the waste water after denitrogenation
Row one-level Fenton oxidation reacts；
D2：The waste water flowed out from one-level Fenton's reaction pond 4110 is delivered to one-level Fenton sedimentation basin 4130, sunk in one-level Fenton
One-level degassing precipitation separation is carried out in shallow lake pond 4130 to the waste water by the reaction of one-level Fenton oxidation；
D3：The waste water flowed out by one-level Fenton sedimentation basin 4130 is delivered to two level Fenton's reaction pond 4120, it is anti-in two level Fenton
Answer in pond 4120 and two level Fenton oxidation reaction is carried out to the waste water for precipitation separation of passing through and deaerate；
D4：The waste water flowed out by two level Fenton's reaction pond 4120 is delivered to two level Fenton sedimentation basin 4140, sunk in two level Fenton
To carrying out two level degassing precipitation separation by the reacted waste water of two level Fenton oxidation in shallow lake pond 4140；
D5：The waste water flowed out from two level Fenton sedimentation basin 4140 is delivered to sand filter 4200, using sand filter 4200 to warp
The waste water crossed after two level degassing precipitation separation carries out sand filtration.
Alternatively, in the step D1, into the Fenton's reaction chamber 4111 in one-level Fenton's reaction pond 4110 add sulfuric acid,
Ferrous sulfate and hydrogen peroxide are stirred, then add flocculant into the Fenton flocculation chamber 4112 in one-level Fenton's reaction pond 4110
It is stirred.In the step D4, sulfuric acid, sulphur are added into the Fenton's reaction chamber 4111 in two level Fenton's reaction pond 4120
Sour ferrous and hydrogen peroxide is stirred, then addition flocculant enters into the Fenton flocculation chamber 4112 in two level Fenton's reaction pond 4120
Row stirring.
The Waste Water Treatment 1 and method of wastewater treatment of cellulose ethanol according to embodiments of the present invention, successively to fiber
Waste water caused by element ethanol carries out anaerobic biodegradation, aeration dephosphorization, denitrogenation and advanced treating, can be by the COD in waste water
Handle below 100mg/L, and it is simple in construction, cost is low, floor space is small.Moreover, fibre according to embodiments of the present invention
The Waste Water Treatment 1 and technique of element ethanol processed are tieed up, not only COD high treating effects, the removal effect of nitrogen phosphorus,
For example, nitrogen can reach below 15mg/L, phosphorus can reach below 0.5mg/L.
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 ",
The orientation or position relationship of the instruction such as " outer ", " clockwise ", " counterclockwise " be based on orientation shown in the drawings or position relationship,
Be for only for ease of the description present invention and simplify description, rather than instruction or imply signified device or element must have it is 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, " first " is defined, the feature of " second " can be expressed
Or implicitly include one or more this feature.In the description of the invention, " multiple " are meant that at least two,
Such as two, three etc., unless otherwise specifically defined.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation "
It should be interpreted broadly Deng term, for example, it may be fixedly connected or be detachably connected, or integrally；Can be
Mechanically connect or electrically connect；Can be joined directly together, can also be indirectly connected by intermediary, can be two
The connection of individual element internal or the interaction relationship of two elements.For the ordinary skill in the art, Ke Yigen
Understand the concrete meaning of above-mentioned term in the present invention according to concrete condition.
In the present invention, unless otherwise clearly defined and limited, fisrt feature second feature it " on " or it " under "
Can directly it be contacted including the first and second features, it is not directly to contact but lead to that can also include the first and second features
The other characterisation contact crossed between them.Moreover, fisrt feature second feature " on ", " top " and " on
Face " includes fisrt feature directly over second feature and oblique upper, or is merely representative of fisrt feature level height higher than the
Two features.Fisrt feature second feature " under ", " lower section " and " below " to include fisrt feature special second
Immediately below sign and obliquely downward, or be merely representative of fisrt feature level height and be 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. mean to combine the specific features of the embodiment or example description, structure, material or
Feature is contained at least one embodiment or example of the present invention.In this manual, to the schematic representation of above-mentioned term
Necessarily it is directed to identical embodiment or example.Moreover, specific features, structure, material or the feature of description can be with
Combined in an appropriate manner in any one or more embodiments or example.In addition, those skilled in the art can incite somebody to action
Different embodiments or example described in this specification are engaged and combined.
Although embodiments of the invention have been shown and described above, it is to be understood that above-described embodiment be it is exemplary,
It is not considered as limiting the invention, one of ordinary skill in the art within the scope of the invention can be to above-described embodiment
It is changed, changes, replacing and modification.
Claims (10)
1. a kind of Waste Water Treatment of cellulose ethanol, it is characterised in that be sequentially connected including waste water treatment process direction
Anaerobic fermentation reaction unit, waste water dephosphorization reaction unit, denitrification reactor and advanced treatment system,
Wherein, the anaerobic fermentation reaction unit includes anaerobic fermentation tank body, stripping tube and air supply pipe, the anaerobic fermentation tank
There is anaerobic reaction room in vivo, the anaerobic reaction room has waste water inlet, delivery port and exhaust outlet, and the stripping tube is located at
In the anaerobic reaction room, lower end of the upper end of the stripping tube with gas outlet and the stripping tube is described with air inlet
Air supply pipe is connected with the air inlet of the stripping tube, for supplying the gas for air lift into the stripping tube；
It is anti-that the waste water dephosphorization reaction unit includes dephosphorization reacting tank body, aerator and degassing precipitation separator, the dephosphorization
Answering in tank body has dephosphorization reative cell, and the dephosphorization reative cell has water inlet and dephosphorization agent adding mouth, and the aerator is set
In the dephosphorization reative cell, the degassing precipitation separator is located in the dephosphorization reative cell and on the aerator
Side, for separating gas and water and sludge.
2. the Waste Water Treatment of cellulose ethanol according to claim 1, it is characterised in that the stripping tube
Lower end extends to the top of the anaerobic reaction room adjacent to the upper end of the bottom of the anaerobic reaction room and the stripping tube, described
Delivery port is located at the top of the anaerobic reaction room and higher than the upper end of the stripping tube.
3. the Waste Water Treatment of cellulose ethanol according to claim 1 or 2, it is characterised in that the air lift
The upper surface of pipe is opened wide to form the gas outlet, and the lower surface of the stripping tube is opened wide to form the air inlet.
4. the Waste Water Treatment of cellulose ethanol according to claim 3, it is characterised in that the stripping tube bag
Include the straight length vertically extended and the segmental arc being connected with the upper end of the straight length, the opening direction of the gas outlet
Angle between vertically downward direction is more than or equal to zero degree and is less than 180 degree.
5. the Waste Water Treatment of cellulose ethanol according to claim 4, it is characterised in that the segmental arc is
Inverted U-shaped, the opening direction of the gas outlet is straight down.
6. the Waste Water Treatment of the cellulose ethanol according to any one of claim 1-5, it is characterised in that institute
Stripping tube is stated to be multiple and be arranged at intervals in the horizontal plane.
7. the Waste Water Treatment of the cellulose ethanol according to any one of claim 1-6, it is characterised in that institute
Stating anaerobic fermentation reaction unit also includes：Separator is precipitated, the precipitation separator is located in the anaerobic reaction room and is located at
Above the stripping tube, the precipitation separator there is the separator delivery port being connected with the delivery port and the delivery port and
The water inlet of the waste water dephosphorization reaction unit is connected.
8. the Waste Water Treatment of cellulose ethanol according to claim 7, it is characterised in that the precipitation separation
Device includes：
Casing, the casing is interior to precipitate chamber formed with degassing, and the bottom of the degassing precipitation chamber has sludge outlet, described to take off
The cross-sectional area of the bottom of gas precipitation 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.
9. the Waste Water Treatment of cellulose ethanol according to claim 8, it is characterised in that limited with the dividing plate
The upper edge for making the box portion of the degassing district is less than the upper edge of the dividing plate and limits the settling zone with the dividing plate
Box portion upper edge.
10. the Waste Water Treatment of cellulose ethanol according to claim 9, it is characterised in that the casing is
Cuboid, the lower end of the first longitudinal side wall of the bottom of the casing extend downward beyond the second longitudinal side wall of the bottom of the casing
Lower 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.
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