CN110668654A - Waste water treatment process for sausage casing processing and heparin extraction - Google Patents
Waste water treatment process for sausage casing processing and heparin extraction Download PDFInfo
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- CN110668654A CN110668654A CN201911063400.6A CN201911063400A CN110668654A CN 110668654 A CN110668654 A CN 110668654A CN 201911063400 A CN201911063400 A CN 201911063400A CN 110668654 A CN110668654 A CN 110668654A
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- 238000000034 method Methods 0.000 title claims abstract description 27
- HTTJABKRGRZYRN-UHFFFAOYSA-N Heparin Chemical compound OC1C(NC(=O)C)C(O)OC(COS(O)(=O)=O)C1OC1C(OS(O)(=O)=O)C(O)C(OC2C(C(OS(O)(=O)=O)C(OC3C(C(O)C(O)C(O3)C(O)=O)OS(O)(=O)=O)C(CO)O2)NS(O)(=O)=O)C(C(O)=O)O1 HTTJABKRGRZYRN-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 229960002897 heparin Drugs 0.000 title claims abstract description 19
- 229920000669 heparin Polymers 0.000 title claims abstract description 19
- 238000012545 processing Methods 0.000 title claims abstract description 19
- 238000000605 extraction Methods 0.000 title claims abstract description 17
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 9
- 235000013580 sausages Nutrition 0.000 title claims description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 112
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 102
- 239000002351 wastewater Substances 0.000 claims abstract description 72
- 238000005273 aeration Methods 0.000 claims abstract description 67
- 238000004062 sedimentation Methods 0.000 claims abstract description 65
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 57
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000010992 reflux Methods 0.000 claims abstract description 19
- 238000005189 flocculation Methods 0.000 claims abstract description 10
- 230000016615 flocculation Effects 0.000 claims abstract description 10
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 8
- 238000000855 fermentation Methods 0.000 claims abstract description 8
- 230000004151 fermentation Effects 0.000 claims abstract description 8
- 239000005708 Sodium hypochlorite Substances 0.000 claims abstract description 4
- 238000005086 pumping Methods 0.000 claims abstract description 4
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000010802 sludge Substances 0.000 claims description 61
- 238000005842 biochemical reaction Methods 0.000 claims description 22
- 239000002131 composite material Substances 0.000 claims description 18
- 239000000969 carrier Substances 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 239000006228 supernatant Substances 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000012065 filter cake Substances 0.000 claims description 3
- 230000002401 inhibitory effect Effects 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 238000004847 absorption spectroscopy Methods 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 235000019737 Animal fat Nutrition 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920001184 polypeptide Polymers 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 102000004196 processed proteins & peptides Human genes 0.000 description 1
- 108090000765 processed proteins & peptides Proteins 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to a waste water treatment process for casing processing and heparin extraction, which comprises the steps of collecting waste water in a collecting tank, pumping the waste water into a DPASB (deep plasma absorption Spectroscopy) by a lifting pump+In the reactor, the wastewater after fermentation automatically flows into a first sedimentation tank for flocculation and sedimentation; then the wastewater enters a stripping tower for ammonia nitrogen stripping, the stripping flows into a second sedimentation tank and a biochemical distribution tank, and the wastewater is heated; the effluent of the distribution tank enters a DPABR anaerobic biological reaction tank I, the effluent of the reaction tank I flows into a DPSBR biological reactor, the effluent of the reactor flows into an intermediate tank, the water temperature is continuously heated, the wastewater in the intermediate tank is lifted to a DPABR anaerobic biological reaction tank II, the effluent of the DPMO aerobic biological reaction tank enters a reflux sedimentation tank, the effluent of the DPABR anaerobic biological reaction tank II automatically flows into an aeration biological filter tank, the effluent of the aeration biological filter tank enters a sedimentation tank III, the effluent of the DPMO anaerobic biological reaction tank enters a break point chlorination tank, and 0.1 percent of sodium hypochlorite is added into the DPSBR biological reaction tank; the effluent of the break point chlorination tank automatically flows into the activated carbon for adsorptionAnd adding carbon powder into the tank to complete the standard discharge.
Description
Technical Field
The invention relates to a waste water treatment process for sausage casing processing and heparin extraction, which is applied to a waste water treatment technology.
Background
Because the salt content, ammonia nitrogen and total nitrogen of the waste water from the processing of the sausage casing and the extraction of the heparin are far beyond the capability of the treatment by the traditional biochemical technology, and the contents of polypeptide, protein and animal fat in the waste water are extremely high, the actual operation effect of the conventional pretreatment methods such as flocculation precipitation is poor, the settleability and hydrophobicity of sludge are poor, and the sludge treatment is also a difficult problem. The method adopted at present for the wastewater is to dilute the wastewater by about 5 to 10 times to reduce the concentrations of the pollutants to the traditional microbial tolerance range and then treat the wastewater according to the conventional mode of flocculation precipitation + UASB + AO. The dilution is illegal, and simultaneously, a large amount of water resources are consumed for dilution, and the pollution discharge cost of enterprises is multiplied; the dosage of the chemicals consumed in the flocculation precipitation link is remarkable, the settleability is poor, the sludge is difficult to filter press, the water content exceeds 93 percent, and the later-stage sludge treatment cost is very high; even if the system is diluted to operate, the operation stability of the system is still extremely poor, the quality of effluent water is difficult to reach the national discharge standard, the system is easy to have the phenomena of sludge expansion and collapse, and the system becomes a serious problem for limiting the survival of the sausage casing and heparin extraction industry.
Disclosure of Invention
The invention aims to: aiming at the defects of the prior art, the process for treating the waste water generated by processing the casing and extracting the heparin is provided, the problem that the waste water is difficult to stably reach the standard in the casing processing and extracting the heparin is solved, and the sustainable development of the casing processing and extracting industry is guaranteed; meanwhile, the comprehensive cost of enterprise wastewater treatment is greatly reduced.
The technical scheme adopted by the invention is as follows: a waste water treatment process for sausage casing processing and heparin extraction comprises the following steps:
step one, collecting waste water in a collecting tank, and arranging a liquid level controller and a lifting pump in the tank;
step two, pumping the wastewater into the DPASB through a lift pump+In the reactor, the wastewater stays in the reactor for 24 hours for fermentation, and the pH value in the equipment is controlled to be not lower than 7.5;
step three, the wastewater after fermentation automatically flows into a first sedimentation tank, PAC and PAM are added for flocculation and sedimentation after the PH value is adjusted to 8.0 in the first sedimentation tank, and most of fixed suspended matters are removed; wherein the adding amount of PAC is 1 percent and the adding amount of PAM is 0.2 percent;
step four, the ammonia nitrogen of the wastewater in the first sedimentation tank reaches 3500mg/L, so that a strong inhibiting effect is caused to a treatment system, the wastewater enters a stripping tower for ammonia nitrogen stripping after the PH value of the wastewater is adjusted to 11 at a water outlet of the first sedimentation tank, the PH value in the denitrification tower is maintained at 11, and the ammonia nitrogen can be reduced to 500mg/L after continuous stripping for 3 hours;
fifthly, enabling the effluent of the stripping tower to flow into a second sedimentation tank, adjusting the pH value of the wastewater back to 7.5 in the second sedimentation tank, and adding 0.5% of PAC and 0.05% of PAM to complete secondary flocculation precipitation; at the moment, water is discharged, and the fixed suspended matters are less than 150 mg/L;
and step six, enabling the effluent of the sedimentation tank II to enter a biochemical water distribution tank, adjusting the pH value of the wastewater to 7.5 in the biochemical water distribution tank, and adjusting the ratio of C to N to P to 300: 5: 1, heating the wastewater to 35 ℃ by adopting steam;
step seven, enabling the effluent of the biochemical distribution tank to enter a first DPABR anaerobic biological reaction tank, controlling the pH value in the first DPABR anaerobic biological reaction tank to be not lower than 7.5, adding 30-80 mesh activated carbon strain carriers and composite biological strains, and enabling the wastewater to stay in the first DPABR anaerobic biological reaction tank for 72 hours to reduce the COD from 12600mg/L to 7560 mg/L;
step eight, enabling the effluent of the first DPABR anaerobic biological reaction tank to flow into a DPSBR bioreactor, adding a 30-80-mesh activated carbon strain carrier and a composite biological strain into the DPSBR bioreactor, reducing COD from 7560mg/L to 1890mg/L, and reducing ammonia nitrogen from 550mg/L to 220 mg/L;
step nine, enabling effluent of the DPSBR bioreactor to flow into an intermediate tank of the DPSBR bioreactor, arranging a liquid level controller and a lifting pump in the intermediate tank, and continuously heating the water temperature to 35 ℃ by adopting steam in the intermediate tank;
step ten, lifting the waste water in the middle pool to a DPABR anaerobic biological reaction pool II through a lifting pump, adding 30-80 meshes of activated carbon strain carriers and composite biological strains into the DPABR anaerobic biological reaction pool II, and staying the waste water for 36 hours to reduce COD (chemical oxygen demand) from 1890mg/L to 1134 mg/L;
step eleven, putting 6-mesh active carbon strain carriers and composite biological strains into a DPMO aerobic biological reaction tank of effluent of a DPABR anaerobic biological reaction tank II, staying the wastewater for 48 hours, and keeping continuous aeration in the tank, wherein the unit can reduce COD from 1134mg/L to 283.5mg/L and reduce ammonia nitrogen from 250mg/L to 100 mg/L;
step twelve, enabling effluent of the DPMO aerobic biological reaction tank to enter a reflux sedimentation tank, completing carrier recovery in the reflux sedimentation tank, and periodically refluxing the carriers to the DPMO aerobic biological reaction tank by using a submersible pump so as to prevent the carriers from losing;
step thirteen, the effluent of the reflux sedimentation tank automatically flows into an aeration biological filter, compound strains are added into the aeration biological filter and continuous aeration is kept, so that the ammonia nitrogen is reduced from 100mg/L to 40 mg/L;
step fourteen, the effluent of the biological aerated filter enters a sedimentation tank III, the sedimentation tank adopts a vertical flow type, the surface load is set to be 0.4, and the fixed suspended matter of the effluent is below 100;
step fifteen, enabling the effluent of the sedimentation tank III to enter a break point chlorination tank, adding 0.1% of sodium hypochlorite into the tank, and staying for 3 hours under hydraulic power to reduce the ammonia nitrogen of the effluent from 40mg/L to 28 mg/L;
sixthly, the effluent of the breakpoint chlorination tank automatically flows into an activated carbon adsorption tank, carbon powder is added into the tank, the COD of the effluent can be reduced from 283.5mg/L to 155.15mg/L, and the ammonia nitrogen can be reduced from 28mg/L to 8mg/L, so that the standard discharge can be completed.
In the present invention: the wastewater stays in the DPSBR bioreactor for 24 hours, then the two DPSBR bioreactors are connected in parallel, the operation is switched, and the 24 hours is 1 period; wherein the reaction time of a single DPSBR bioreactor is 12 hours of water inlet, aeration is carried out while water inlet is carried out, aeration reaction is continued for 8 hours after water inlet is stopped, aeration natural sedimentation is stopped for 3 hours, water is discharged for 1 hour, and all 12 hours of water inlet is discharged into the intermediate tank within 1 hour.
In the present invention: the stripping tower efficiently removes ammonia nitrogen, and part of effluent water in the intermediate tank and the reflux sedimentation tank flows back to the ammonia stripping tower to further degrade the ammonia nitrogen, so that the ammonia nitrogen and total nitrogen of biochemical influent water are effectively ensured to be as low as possible.
In the present invention: the first sedimentation tank, the second sedimentation tank, the first DPABR anaerobic biological reaction tank and the DPASB+And the sludge in the reactor, the DPABR anaerobic biological reaction tank II, the reflux sedimentation tank and the sedimentation tank III is conveyed into a sludge concentration tank through sludge pipelines, and then the sludge is compressed and then a filter cake is transported outside.
In the present invention: the DPMO aerobic biological reaction tank comprises a DPMO reaction tank main body, an aeration fan, a water inlet pipe, an aeration pipe and a sludge discharge pipe, wherein the aeration pipe and the sludge discharge pipe are arranged in the DPMO reaction tank main body; a water inlet pipe is arranged on one side of the DPMO reaction tank main body, an overflow water outlet is arranged on the other side of the DPMO reaction tank main body, a 30-60-mesh activated carbon strain carrier is arranged in the DPMO reaction tank main body, and composite strains are arranged on the activated carbon strain carrier.
In the present invention: the DPSBR bioreactor comprises a DPSBR reaction tank main body, an aeration fan, a water inlet pipe, an aeration pipe, a sludge discharge pipe and an intermediate tank, wherein the DPSBR reaction tank main body is internally provided with the aeration pipe and the sludge discharge pipe, the aeration pipe is positioned at the bottom of the DPSBR reaction tank main body and is connected with the aeration fan through an aeration connecting pipe, and the sludge discharge pipe discharges sludge in the DPSBR reaction tank main body out of the tank through a sludge pump; a water inlet pipe is arranged on one side of the DPSBR reaction tank main body, a decanter is arranged on the other side of the DPSBR reaction tank main body, an active carbon strain carrier of 30-60 meshes is arranged in the DPSBR reaction tank main body, and a composite strain is arranged on the active carbon strain carrier; a communicating pipe is arranged between the DPSBR reaction tank main body and the intermediate tank, and supernatant in the DPSBR reaction tank main body is discharged into the intermediate tank through the matching of a decanter and the communicating pipe.
In the present invention: the first DPABR anaerobic biological reaction tank and the second DPABR anaerobic biological reaction tank comprise a DPABR anaerobic biological reaction tank body, four biochemical reaction tanks are arranged in the DPABR anaerobic biological reaction tank body, every two of the four biochemical reaction tanks are connected through a filter frame and a water distribution pipe, a water inlet pipe is arranged on the side surface of the top of the first biochemical reaction tank, and an overflow weir is arranged on the upper part of the fourth biochemical reaction tank; each biochemical pool is internally provided with a bearing plate, and a strain carrier layer is arranged on the bearing plate; the bottom of the biochemical reaction tank is provided with a sludge discharge pipe and an aeration pipe.
In the present invention: the DPASB+The reactor comprises a reactor body, a water seal tank is arranged at the upper end of the reactor body, and the reaction is carried outOne side of the reactor body is provided with a water inlet pipe, the other side of the reactor body is provided with a water outlet, the water inlet pipe extends into the reactor body, the water inlet pipe is provided with a water distributor and a reflecting plate, the upper end in the reactor body is provided with a three-phase separator and is fixed through a fixing support, and a cross water collecting tank is arranged on the upper end of the reactor body and is connected with the water outlet.
After the technical scheme is adopted, the invention has the beneficial effects that: the invention has reasonable design and simple process, solves the problem that the sausage casing processing and heparin extraction wastewater field can not be stably treated to reach the standard, fills the technical blank, thoroughly solves the problems of poor pretreatment effect, large sludge amount and poor precipitability, and has more stable treatment of modified biochemical sludge, good filter pressing effect and water content lower than 70 percent; the method solves the problem of stability of the biochemical treatment system in a high-salinity environment, realizes standard control on total nitrogen and ammonia nitrogen in a targeted manner, and thoroughly solves the problem of removal of strong inhibition factors of the biochemical system by the high-ammonia nitrogen.
Drawings
FIG. 1 is a schematic flow diagram of the present invention;
FIG. 2 is a schematic diagram of a DPMO aerobiont reaction tank according to the present invention;
FIG. 3 is a schematic diagram of a DPSBR bioreactor in accordance with the present invention;
FIG. 4 is a schematic structural diagram of a DPABR anaerobic biological reaction tank in the invention;
FIG. 5 shows a DPASB of the present invention+The structure of the fermentation reactor is shown schematically.
In the figure: 1. an aeration fan; 2. an overflow drain port; 3. a water inlet pipe; 4, a DPMO reaction tank main body; 5. an activated carbon strain carrier; 6. an aeration pipe; 7. an aeration connecting pipe; 8. a sludge discharge pipe; 9, a DPSBR reaction tank main body; 10. decanting device; 11. a middle water tank; 12, a DPABR anaerobic biological reaction tank body; 13. a support plate; 14. a biochemical reaction tank; 15. a filter frame; 17. an overflow weir; 18. a strain carrier layer; 19. a water distribution pipe; 20. a reactor body; 21. fixing a bracket; 22. a reflective plate; 23. a water distributor; 24. a three-phase separator; 25. a cross water collecting tank; 26. a water outlet; 27. and (6) sealing the tank with water.
Detailed Description
The invention will be further described with reference to the accompanying drawings.
As shown in figure 1, the waste water treatment process for sausage casing processing and heparin extraction comprises the following steps:
step one, collecting waste water in a collecting tank, and arranging a liquid level controller and a lifting pump in the tank;
step two, pumping the wastewater into the DPASB through a lift pump+In the reactor, the wastewater stays in the reactor for 24 hours for fermentation, and the pH value in the equipment is controlled to be not lower than 7.5;
step three, the wastewater after fermentation automatically flows into a first sedimentation tank, PAC and PAM are added for flocculation and sedimentation after the PH value is adjusted to 8.0 in the first sedimentation tank, and most of fixed suspended matters are removed; wherein the adding amount of PAC is 1 percent and the adding amount of PAM is 0.2 percent;
step four, the ammonia nitrogen of the wastewater in the first sedimentation tank reaches 3500mg/L, so that a strong inhibiting effect is caused to a treatment system, the wastewater enters a stripping tower for ammonia nitrogen stripping after the PH value of the wastewater is adjusted to 11 at a water outlet of the first sedimentation tank, the PH value in the denitrification tower is maintained at 11, and the ammonia nitrogen can be reduced to 500mg/L after continuous stripping for 3 hours;
fifthly, enabling the effluent of the stripping tower to flow into a second sedimentation tank, adjusting the pH value of the wastewater back to 7.5 in the second sedimentation tank, and adding 0.5% of PAC and 0.05% of PAM to complete secondary flocculation precipitation; at the moment, water is discharged, and the fixed suspended matters are less than 150 mg/L; the stripping tower efficiently removes ammonia nitrogen, and part of effluent water in the intermediate tank and the reflux sedimentation tank flows back to the ammonia stripping tower to further degrade the ammonia nitrogen, so that the ammonia nitrogen and total nitrogen of biochemical influent water are effectively ensured to be as low as possible;
and step six, enabling the effluent of the sedimentation tank II to enter a biochemical water distribution tank, adjusting the pH value of the wastewater to 7.5 in the biochemical water distribution tank, and adjusting the ratio of C to N to P to 300: 5: 1, heating the wastewater to 35 ℃ by adopting steam;
step seven, enabling the effluent of the biochemical distribution tank to enter a first DPABR anaerobic biological reaction tank, controlling the pH value in the first DPABR anaerobic biological reaction tank to be not lower than 7.5, adding 30-80 mesh activated carbon strain carriers and composite biological strains, and enabling the wastewater to stay in the first DPABR anaerobic biological reaction tank for 72 hours to reduce the COD from 12600mg/L to 7560 mg/L;
step eight, enabling the effluent of the first DPABR anaerobic biological reaction tank to flow into a DPSBR bioreactor, adding a 30-80-mesh activated carbon strain carrier and a composite biological strain into the DPSBR bioreactor, reducing COD from 7560mg/L to 1890mg/L, and reducing ammonia nitrogen from 550mg/L to 220 mg/L; the wastewater stays in the DPSBR bioreactor for 24 hours, then the two DPSBR bioreactors are connected in parallel, the operation is switched, and the 24 hours is 1 period; wherein the reaction time of a single DPSBR bioreactor is 12 hours of water inflow, aeration is carried out while water inflow is carried out, aeration reaction is continued for 8 hours after water inflow is stopped, aeration natural sedimentation is stopped for 3 hours, water is discharged for 1 hour, and 12 hours of water inflow is completely discharged into an intermediate tank within 1 hour;
step nine, enabling effluent of the DPSBR bioreactor to flow into an intermediate tank of the DPSBR bioreactor, arranging a liquid level controller and a lifting pump in the intermediate tank, and continuously heating the water temperature to 35 ℃ by adopting steam in the intermediate tank;
step ten, lifting the waste water in the middle pool to a DPABR anaerobic biological reaction pool II through a lifting pump, adding 30-80 meshes of activated carbon strain carriers and composite biological strains into the DPABR anaerobic biological reaction pool II, and staying the waste water for 36 hours to reduce COD (chemical oxygen demand) from 1890mg/L to 1134 mg/L;
step eleven, putting 6-mesh active carbon strain carriers and composite biological strains into a DPMO aerobic biological reaction tank of effluent of a DPABR anaerobic biological reaction tank II, staying the wastewater for 48 hours, and keeping continuous aeration in the tank, wherein the unit can reduce COD from 1134mg/L to 283.5mg/L and reduce ammonia nitrogen from 250mg/L to 100 mg/L;
step twelve, enabling effluent of the DPMO aerobic biological reaction tank to enter a reflux sedimentation tank, completing carrier recovery in the reflux sedimentation tank, and periodically refluxing the carriers to the DPMO aerobic biological reaction tank by using a submersible pump so as to prevent the carriers from losing;
step thirteen, the effluent of the reflux sedimentation tank automatically flows into an aeration biological filter, compound strains are added into the aeration biological filter and continuous aeration is kept, so that the ammonia nitrogen is reduced from 100mg/L to 40 mg/L;
step fourteen, the effluent of the biological aerated filter enters a sedimentation tank III, the sedimentation tank adopts a vertical flow type, the surface load is set to be 0.4, and the fixed suspended matter of the effluent is below 100;
step fifteen, enabling the effluent of the sedimentation tank III to enter a break point chlorination tank, adding 0.1% of sodium hypochlorite into the tank, and staying for 3 hours under hydraulic power to reduce the ammonia nitrogen of the effluent from 40mg/L to 28 mg/L;
sixthly, the effluent of the breakpoint chlorination tank automatically flows into an activated carbon adsorption tank, carbon powder is added into the tank, the COD of the effluent can be reduced from 283.5mg/L to 155.15mg/L, and the ammonia nitrogen can be reduced from 28mg/L to 8mg/L, so that the standard discharge can be completed.
In the technical scheme, the first sedimentation tank, the second sedimentation tank, the first DPABR anaerobic biological reaction tank and the DPASB+And the sludge in the reactor, the DPABR anaerobic biological reaction tank II, the reflux sedimentation tank and the sedimentation tank III is conveyed into a sludge concentration tank through sludge pipelines, and then the sludge is compressed and then a filter cake is transported outside.
As shown in fig. 2, the DPMO aerobic biological reaction tank comprises a DPMO reaction tank main body 4, an aeration fan 1, a water inlet pipe 3, an aeration pipe 6 and a sludge discharge pipe 8, wherein the aeration pipe 6 and the sludge discharge pipe 8 are arranged in the DPMO reaction tank main body 4, the aeration pipe 6 is positioned at the bottom of the DPMO reaction tank main body 4 and is connected with the aeration fan 1 through an aeration connecting pipe 7, and the sludge discharge pipe 8 discharges sludge in the DPMO reaction tank main body 4 out of the tank through a sludge pump; a water inlet pipe 3 is arranged on one side of the DPMO reaction tank main body 4, an overflow outlet 2 is arranged on the other side of the DPMO reaction tank main body 4, a 30-60 mesh activated carbon strain carrier 5 is arranged in the DPMO reaction tank main body 4, and the adding amount is 0.05KG/m3The tank capacity is that the activated carbon strain carrier 5 is provided with compound strains. Continuously feeding water and continuously discharging water, continuously operating the aeration fan 1 to maintain the concentration of dissolved oxygen in the tank, and regularly discharging sludge according to the sludge concentration condition.
As shown in fig. 3, the DPSBR bioreactor comprises a DPSBR reaction tank main body 9, an aeration fan 1, a water inlet pipe 3, an aeration pipe 6, a sludge discharge pipe 8 and an intermediate tank 11, wherein the aeration pipe 6 and the sludge discharge pipe 8 are arranged in the DPSBR reaction tank main body 9, the aeration pipe 6 is positioned at the bottom of the DPSBR reaction tank main body 9 and is connected with the aeration fan 1 through an aeration connecting pipe 7, and the sludge discharge pipe 8 discharges sludge in the DPSBR reaction tank main body 9 out of the tank through a sludge pump; the DPSBR reactionOne side of the tank main body 9 is provided with a water inlet pipe 3, the other side is provided with a decanter 10, the DPSBR reaction tank main body 9 is internally provided with a 30-60 mesh activated carbon strain carrier 5, and the adding amount is 0.05KG/m3The tank capacity is that the activated carbon strain carrier 5 is provided with composite strains, the adding amount of the strains is 0.2KG strains/m3The volume of the pool; wherein a communicating pipe is arranged between the DPSBR reaction tank main body 9 and the intermediate tank 11, and supernatant in the DPSBR reaction tank main body 9 is discharged into the intermediate tank 11 through the matching of a decanter 10 and the communicating pipe.
Firstly, continuously feeding water for 12 hours through the water inlet pipe 3, starting the aeration fan 1 to perform continuous aeration simultaneously when water is fed, continuing aeration for 8 hours after water feeding is completed, standing and precipitating for 3 hours after aeration is completed, and finally starting the decanter 10 to discharge supernatant to the intermediate tank 11. And (4) starting a sludge pump to discharge sludge regularly according to the sludge concentration.
As shown in fig. 4, the DPABR anaerobic biological reaction tank i and the DPABR anaerobic biological reaction tank ii are DPABR anaerobic biological reaction tanks with the same structure, and comprise a DPABR anaerobic biological reaction tank body 12, four biochemical reaction tanks 14 are arranged in the DPABR anaerobic biological reaction tank body 12, every two of the four biochemical reaction tanks 14 are connected through a filter frame 15 and a water distribution pipe 19, a water inlet pipe 3 is arranged on the side surface of the top of the first biochemical reaction tank 14, and an overflow weir 17 is arranged on the upper part of the fourth biochemical reaction tank 14; a bearing plate 13 is arranged in each biochemical pool 14, and a strain carrier layer 18 is arranged on the bearing plate 13; the bottom of the biochemical reaction tank 14 is provided with a sludge discharge pipe 8 and an aeration pipe 6.
The first grid biochemical reaction tank 14 is introduced with water from the water inlet pipe 3 on the top side, is guided to the bottom of the tank by a pipeline for uniform water distribution, is fully contacted and degraded with strains by a strain carrier layer 18, overflows into the water distribution pipe 19 to the next grid biochemical reaction tank 14 through the filter frame 15, is wholly in a plug flow state, is in an upflow state in each grid, and is collected and discharged from an overflow weir 17 of the biochemical reaction tank 14 in the fourth grid after the wastewater is biologically degraded in the biochemical reaction tank 14 in the fourth grid. Adding strain carrier into the four-grid biochemical reaction tank 14, wherein the carrier is activated carbon which is a special carrier for 1-6 meshes of strains, and the adding amount is 0.05 ton/m3(ii) a And adding the composite strain into the biochemical reaction tank 14The addition amount is 0.2KG/m3。
As shown in fig. 5, the DPASB+The reactor comprises a reactor body 20, a water seal tank 27 is arranged at the upper end of the reactor body 20, a water inlet pipe 3 is arranged at one side of the reactor body 20, a water outlet 26 is arranged at the other side of the reactor body 20, the water inlet pipe 3 extends into the reactor body 20, a water distributor 23 and a reflecting plate 22 are arranged on the water inlet pipe 3, a three-phase separator 24 is arranged at the upper end in the reactor body 20 and is fixed through a fixing support 21, and a cross water collecting tank 25 is arranged at the upper end connected with the water outlet 26.
In operation, wastewater enters the reactor body 20 from the water inlet pipe 3, and flows out downwards uniformly through the water distributor 23, so that in order to prevent turbulence at the bottom, the water flow is homogenized on the surface of the reflecting plate 22, thereby achieving the effect of uniform water flow in a plane. The whole body of the wastewater and the sludge in the reactor body 20 is in a plug flow state towards the top of the reactor, and organic matters in the wastewater are fully contacted with microorganisms in the water pushing process and are degraded. Due to the self-weight of the granular sludge, the sludge can be maintained to form a sludge bed in the middle and lower part of the reactor body 20 during the upward plug flow. When the degraded wastewater, part of the sludge and methane gas rise to the three-phase separator 24, the methane gas is collected and discharged from the exhaust port of the water seal tank 27, the sludge is blocked in the reactor and settled, and the degraded wastewater is collected by the cross-shaped water collection tank 25 and discharged from the water discharge port 26.
The above description is directed to specific embodiments of the present invention, but the present invention is not limited to the above description. Any equivalent modifications and alterations to this technical solution would be considered within the scope of this invention by those skilled in the art. Accordingly, equivalent changes and modifications made without departing from the spirit and scope of the present invention should be covered by the present invention.
Claims (8)
1. A waste water treatment process for sausage casing processing and heparin extraction is characterized in that: the method comprises the following steps:
step one, collecting waste water in a collecting tank, and arranging a liquid level controller and a lifting pump in the tank;
step two, pumping the wastewater into the DPASB through a lift pump+In the reactor, the wastewater stays in the reactor for 24 hours for fermentation, and the pH value in the equipment is controlled to be not lower than 7.5;
step three, the wastewater after fermentation automatically flows into a first sedimentation tank, PAC and PAM are added for flocculation and sedimentation after the PH value is adjusted to 8.0 in the first sedimentation tank, and most of fixed suspended matters are removed; wherein the adding amount of PAC is 1 percent and the adding amount of PAM is 0.2 percent;
step four, the ammonia nitrogen of the wastewater in the first sedimentation tank reaches 3500mg/L, so that a strong inhibiting effect is caused to a treatment system, the wastewater enters a stripping tower for ammonia nitrogen stripping after the PH value of the wastewater is adjusted to 11 at a water outlet of the first sedimentation tank, the PH value in the denitrification tower is maintained at 11, and the ammonia nitrogen can be reduced to 500mg/L after continuous stripping for 3 hours;
fifthly, enabling the effluent of the stripping tower to flow into a second sedimentation tank, adjusting the pH value of the wastewater back to 7.5 in the second sedimentation tank, and adding 0.5% of PAC and 0.05% of PAM to complete secondary flocculation precipitation; at the moment, water is discharged, and the fixed suspended matters are less than 150 mg/L;
and step six, enabling the effluent of the sedimentation tank II to enter a biochemical water distribution tank, adjusting the pH value of the wastewater to 7.5 in the biochemical water distribution tank, and adjusting the ratio of C to N to P to 300: 5: 1, heating the wastewater to 35 ℃ by adopting steam;
step seven, enabling the effluent of the biochemical distribution tank to enter a first DPABR anaerobic biological reaction tank, controlling the pH value in the first DPABR anaerobic biological reaction tank to be not lower than 7.5, adding 30-80 mesh activated carbon strain carriers and composite biological strains, and enabling the wastewater to stay in the first DPABR anaerobic biological reaction tank for 72 hours to reduce the COD from 12600mg/L to 7560 mg/L;
step eight, enabling the effluent of the first DPABR anaerobic biological reaction tank to flow into a DPSBR bioreactor, adding a 30-80-mesh activated carbon strain carrier and a composite biological strain into the DPSBR bioreactor, reducing COD from 7560mg/L to 1890mg/L, and reducing ammonia nitrogen from 550mg/L to 220 mg/L;
step nine, enabling effluent of the DPSBR bioreactor to flow into an intermediate tank of the DPSBR bioreactor, arranging a liquid level controller and a lifting pump in the intermediate tank, and continuously heating the water temperature to 35 ℃ by adopting steam in the intermediate tank;
step ten, lifting the waste water in the middle pool to a DPABR anaerobic biological reaction pool II through a lifting pump, adding 30-80 meshes of activated carbon strain carriers and composite biological strains into the DPABR anaerobic biological reaction pool II, and staying the waste water for 36 hours to reduce COD (chemical oxygen demand) from 1890mg/L to 1134 mg/L;
step eleven, putting 6-mesh active carbon strain carriers and composite biological strains into a DPMO aerobic biological reaction tank of effluent of a DPABR anaerobic biological reaction tank II, staying the wastewater for 48 hours, and keeping continuous aeration in the tank, wherein the unit can reduce COD from 1134mg/L to 283.5mg/L and reduce ammonia nitrogen from 250mg/L to 100 mg/L;
step twelve, enabling effluent of the DPMO aerobic biological reaction tank to enter a reflux sedimentation tank, completing carrier recovery in the reflux sedimentation tank, and periodically refluxing the carriers to the DPMO aerobic biological reaction tank by using a submersible pump so as to prevent the carriers from losing;
step thirteen, the effluent of the reflux sedimentation tank automatically flows into an aeration biological filter, compound strains are added into the aeration biological filter and continuous aeration is kept, so that the ammonia nitrogen is reduced from 100mg/L to 40 mg/L;
step fourteen, the effluent of the biological aerated filter enters a sedimentation tank III, the sedimentation tank adopts a vertical flow type, the surface load is set to be 0.4, and the fixed suspended matter of the effluent is below 100;
step fifteen, enabling the effluent of the sedimentation tank III to enter a break point chlorination tank, adding 0.1% of sodium hypochlorite into the tank, and staying for 3 hours under hydraulic power to reduce the ammonia nitrogen of the effluent from 40mg/L to 28 mg/L;
sixthly, the effluent of the breakpoint chlorination tank automatically flows into an activated carbon adsorption tank, carbon powder is added into the tank, the COD of the effluent can be reduced from 283.5mg/L to 155.15mg/L, and the ammonia nitrogen can be reduced from 28mg/L to 8mg/L, so that the standard discharge can be completed.
2. The process of claim 1 for treating waste water from casing processing and heparin extraction, wherein the process comprises the following steps: the wastewater stays in the DPSBR bioreactor for 24 hours, then the two DPSBR bioreactors are connected in parallel, the operation is switched, and the 24 hours is 1 period; wherein the reaction time of a single DPSBR bioreactor is 12 hours of water inlet, aeration is carried out while water inlet is carried out, aeration reaction is continued for 8 hours after water inlet is stopped, aeration natural sedimentation is stopped for 3 hours, water is discharged for 1 hour, and all 12 hours of water inlet is discharged into the intermediate tank within 1 hour.
3. The process of claim 1 for treating waste water from casing processing and heparin extraction, wherein the process comprises the following steps: the stripping tower efficiently removes ammonia nitrogen, and part of effluent water in the intermediate tank and the reflux sedimentation tank flows back to the ammonia stripping tower to further degrade the ammonia nitrogen, thereby more effectively ensuring that the ammonia nitrogen and total nitrogen of biochemical influent water are as low as possible。
4. The process of claim 1 for treating waste water from casing processing and heparin extraction, wherein the process comprises the following steps: the first sedimentation tank, the second sedimentation tank, the first DPABR anaerobic biological reaction tank and the DPASB+And the sludge in the reactor, the DPABR anaerobic biological reaction tank II, the reflux sedimentation tank and the sedimentation tank III is conveyed into a sludge concentration tank through sludge pipelines, and then the sludge is compressed and then a filter cake is transported outside.
5. The process of claim 1 for treating waste water from casing processing and heparin extraction, wherein the process comprises the following steps: the DPMO aerobic biological reaction tank comprises a DPMO reaction tank main body (4), an aeration fan (1), a water inlet pipe (3), an aeration pipe (6) and a sludge discharge pipe (8), wherein the aeration pipe (6) and the sludge discharge pipe (8) are arranged in the DPMO reaction tank main body (4), the aeration pipe (6) is positioned at the bottom of the DPMO reaction tank main body (4) and is connected with the aeration fan (1) through an aeration connecting pipe (7), and the sludge discharge pipe (8) discharges sludge in the DPMO reaction tank main body (4) out of the tank through a sludge pump; one side of the DPMO reaction tank main body (4) is provided with a water inlet pipe (3), the other side of the DPMO reaction tank main body is provided with an overflow outlet (2), the DPMO reaction tank main body (4) is internally provided with a 30-60-mesh activated carbon strain carrier (5), and the activated carbon strain carrier (5) is provided with composite strains.
6. The process of claim 1 for treating waste water from casing processing and heparin extraction, wherein the process comprises the following steps: the DPSBR bioreactor comprises a DPSBR reaction tank main body (9), an aeration fan (1), a water inlet pipe (3), an aeration pipe (6), a sludge discharge pipe (8) and a middle tank (11), wherein the DPSBR reaction tank main body (9) is internally provided with the aeration pipe (6) and the sludge discharge pipe (8), the aeration pipe (6) is positioned at the bottom of the DPSBR reaction tank main body (9) and is connected with the aeration fan (1) through an aeration connecting pipe (7), and the sludge discharge pipe (8) discharges sludge in the DPSBR reaction tank main body (9) out of the tank through a sludge pump; a water inlet pipe (3) is arranged on one side of the DPSBR reaction tank main body (9), a decanter (10) is arranged on the other side of the DPSBR reaction tank main body, an active carbon strain carrier (5) with 30-60 meshes is arranged in the DPSBR reaction tank main body (9), and a composite strain is arranged on the active carbon strain carrier (5); wherein a communicating pipe is arranged between the DPSBR reaction tank main body (9) and the intermediate tank (11), and supernatant in the DPSBR reaction tank main body (9) is discharged into the intermediate tank (11) through the matching of a decanter (10) and the communicating pipe.
7. The process of claim 1 for treating waste water from casing processing and heparin extraction, wherein the process comprises the following steps: the first DPABR anaerobic biological reaction tank and the second DPABR anaerobic biological reaction tank comprise DPABR anaerobic biological reaction tank bodies (12), four biochemical reaction tanks (14) are arranged in the DPABR anaerobic biological reaction tank bodies (12), every two of the four biochemical reaction tanks (14) are connected through a filter frame (15) and a water distribution pipe (19), a water inlet pipe (3) is arranged on the side surface of the top of the first biochemical reaction tank (14), and an overflow weir (17) is arranged on the upper part of the fourth biochemical reaction tank (14); a bearing plate (13) is arranged in each biochemical pool (14), and a strain carrier layer (18) is arranged on the bearing plate (13); the bottom of the biochemical reaction tank (14) is provided with a sludge discharge pipe (8) and an aeration pipe (6).
8. The process of claim 1 for treating waste water from casing processing and heparin extraction, wherein the process comprises the following steps: the DPASB+The reactor comprises a reactor body (20) The utility model discloses a reactor, the upper end of reactor body (20) is equipped with water-sealed tank (27), and one side of reactor body (20) is equipped with inlet tube (3), and the opposite side is equipped with outlet (26), inlet tube (3) extend and get into in reactor body (20), inlet tube (3) on be equipped with water-locator (23) and reflecting plate (22), reactor body (20) in the upper end be equipped with three-phase separator (24) to fix through fixed bolster (21), wherein link to each other with outlet (26) and be equipped with cross water catch bowl (25).
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Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000093998A (en) * | 1998-09-26 | 2000-04-04 | Korea Advanced Inst Of Sci Technol | Method and apparatus for treating high-concentration waste water |
| CN101830602A (en) * | 2010-05-18 | 2010-09-15 | 沈阳石蜡化工有限公司 | Biochemical treatment method of acrylic ester industrial wastewater |
| WO2010133151A1 (en) * | 2009-05-21 | 2010-11-25 | 潍坊金丝达印染有限公司 | Organic wastewater recycling treatment method |
| CN102690026A (en) * | 2012-06-18 | 2012-09-26 | 哈尔滨工业大学 | Method for treating waste water generated in casing production |
| CN103073149A (en) * | 2012-12-05 | 2013-05-01 | 浙江省环境工程有限公司 | Harmless processing method of night soil |
| CN103342441A (en) * | 2013-07-05 | 2013-10-09 | 伊犁川宁生物技术有限公司 | Erythromycin thiocyanate wastewater treatment method |
| CN203976576U (en) * | 2014-05-05 | 2014-12-03 | 浙江海洋学院 | Kitchen waste water treatment system |
| CN204174050U (en) * | 2014-10-11 | 2015-02-25 | 南京万德斯环保科技有限公司 | A kind for the treatment of unit of high ammonia nitrogen organic waste water |
| CN104671597A (en) * | 2015-01-29 | 2015-06-03 | 浦城正大生化有限公司 | Treatment process of antibiotic wastewater |
| CN104787968A (en) * | 2015-04-03 | 2015-07-22 | 常州大学 | Aureomycin waste water treatment system |
| CN107337321A (en) * | 2017-08-11 | 2017-11-10 | 中机国际工程设计研究院有限责任公司 | Anaerobic digestion of kitchen wastes wastewater treatment equipment |
| CN109534612A (en) * | 2018-12-26 | 2019-03-29 | 唐山中溶科技有限公司 | Bio-ethanol anaerobic waste water denitrification system |
-
2019
- 2019-11-04 CN CN201911063400.6A patent/CN110668654A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000093998A (en) * | 1998-09-26 | 2000-04-04 | Korea Advanced Inst Of Sci Technol | Method and apparatus for treating high-concentration waste water |
| WO2010133151A1 (en) * | 2009-05-21 | 2010-11-25 | 潍坊金丝达印染有限公司 | Organic wastewater recycling treatment method |
| CN101830602A (en) * | 2010-05-18 | 2010-09-15 | 沈阳石蜡化工有限公司 | Biochemical treatment method of acrylic ester industrial wastewater |
| CN102690026A (en) * | 2012-06-18 | 2012-09-26 | 哈尔滨工业大学 | Method for treating waste water generated in casing production |
| CN103073149A (en) * | 2012-12-05 | 2013-05-01 | 浙江省环境工程有限公司 | Harmless processing method of night soil |
| CN103342441A (en) * | 2013-07-05 | 2013-10-09 | 伊犁川宁生物技术有限公司 | Erythromycin thiocyanate wastewater treatment method |
| CN203976576U (en) * | 2014-05-05 | 2014-12-03 | 浙江海洋学院 | Kitchen waste water treatment system |
| CN204174050U (en) * | 2014-10-11 | 2015-02-25 | 南京万德斯环保科技有限公司 | A kind for the treatment of unit of high ammonia nitrogen organic waste water |
| CN104671597A (en) * | 2015-01-29 | 2015-06-03 | 浦城正大生化有限公司 | Treatment process of antibiotic wastewater |
| CN104787968A (en) * | 2015-04-03 | 2015-07-22 | 常州大学 | Aureomycin waste water treatment system |
| CN107337321A (en) * | 2017-08-11 | 2017-11-10 | 中机国际工程设计研究院有限责任公司 | Anaerobic digestion of kitchen wastes wastewater treatment equipment |
| CN109534612A (en) * | 2018-12-26 | 2019-03-29 | 唐山中溶科技有限公司 | Bio-ethanol anaerobic waste water denitrification system |
Non-Patent Citations (1)
| Title |
|---|
| 马伟文: "给排水科学与工程实验技术", 华南理工大学出版社 * |
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