CN103011504A - Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide - Google Patents
Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide Download PDFInfo
- Publication number
- CN103011504A CN103011504A CN2012105269960A CN201210526996A CN103011504A CN 103011504 A CN103011504 A CN 103011504A CN 2012105269960 A CN2012105269960 A CN 2012105269960A CN 201210526996 A CN201210526996 A CN 201210526996A CN 103011504 A CN103011504 A CN 103011504A
- Authority
- CN
- China
- Prior art keywords
- sludge
- waste water
- nosiheptide
- tank
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 80
- 239000002351 wastewater Substances 0.000 title claims abstract description 72
- FPTCMHOCGKKRGQ-WYOWUDGCSA-N Multhiomycin Natural products CC=C1NC(=O)[C@@H](NC(=O)c2csc(n2)c3cc(O)c(nc3c4csc(n4)[C@H]5CSC(=O)c6[nH]c7cccc(COC(=O)[C@@H](O)C[C@H](NC(=O)c8csc1n8)c9nc(cs9)C(=O)N5)c7c6C)c%10nc(cs%10)C(=O)N[C@@H](C)C(=O)N)[C@H](C)O FPTCMHOCGKKRGQ-WYOWUDGCSA-N 0.000 title claims abstract description 66
- 101800003864 Nosiheptide Proteins 0.000 title claims abstract description 66
- MQWDKYHFGBWGQZ-JQTJYXGUSA-N nosiheptide Chemical compound N([C@H](C(=O)N\C(C=1SC=C(N=1)C(=O)N[C@@H]1CC(O)C(=O)OCC=2C=CC=C3NC(=C(C3=2)C)C(=O)SC[C@H](NC(=O)C=2N=C1SC=2)C=1SC=C(N=1)C1=N2)=C/C)[C@@H](C)O)C(=O)C(N=3)=CSC=3C1=CC(=O)\C2=C1/NC(C(=O)NC(=C)C(N)=O)=CS1 MQWDKYHFGBWGQZ-JQTJYXGUSA-N 0.000 title claims abstract description 66
- 229950006423 nosiheptide Drugs 0.000 title claims abstract description 66
- 238000009776 industrial production Methods 0.000 title claims abstract description 18
- 238000000855 fermentation Methods 0.000 title abstract description 18
- 230000004151 fermentation Effects 0.000 title abstract description 18
- 125000004122 cyclic group Chemical group 0.000 title abstract 2
- 239000010802 sludge Substances 0.000 claims abstract description 125
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 97
- 238000005842 biochemical reaction Methods 0.000 claims abstract description 67
- 238000011282 treatment Methods 0.000 claims abstract description 67
- 230000008569 process Effects 0.000 claims abstract description 53
- 238000011221 initial treatment Methods 0.000 claims abstract description 29
- 239000012528 membrane Substances 0.000 claims abstract description 18
- 239000007787 solid Substances 0.000 claims abstract description 17
- 241000187762 Streptomyces actuosus Species 0.000 claims abstract description 12
- 239000000126 substance Substances 0.000 claims abstract description 11
- 230000018044 dehydration Effects 0.000 claims abstract description 3
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 3
- 239000002921 fermentation waste Substances 0.000 claims description 49
- 239000007788 liquid Substances 0.000 claims description 30
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 21
- 239000012533 medium component Substances 0.000 claims description 21
- 235000010469 Glycine max Nutrition 0.000 claims description 18
- 244000068988 Glycine max Species 0.000 claims description 18
- 239000006052 feed supplement Substances 0.000 claims description 17
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 16
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 16
- 238000005273 aeration Methods 0.000 claims description 14
- 238000001914 filtration Methods 0.000 claims description 14
- 238000010992 reflux Methods 0.000 claims description 14
- 239000003995 emulsifying agent Substances 0.000 claims description 11
- 230000002000 scavenging effect Effects 0.000 claims description 11
- 239000000843 powder Substances 0.000 claims description 9
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 8
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 8
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 8
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000013461 design Methods 0.000 claims description 8
- ZPWVASYFFYYZEW-UHFFFAOYSA-L dipotassium hydrogen phosphate Chemical compound [K+].[K+].OP([O-])([O-])=O ZPWVASYFFYYZEW-UHFFFAOYSA-L 0.000 claims description 8
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 8
- 235000017550 sodium carbonate Nutrition 0.000 claims description 8
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 8
- 235000011152 sodium sulphate Nutrition 0.000 claims description 8
- 239000000706 filtrate Substances 0.000 claims description 7
- 230000004907 flux Effects 0.000 claims description 7
- 238000011068 loading method Methods 0.000 claims description 7
- 238000010899 nucleation Methods 0.000 claims description 7
- 235000006408 oxalic acid Nutrition 0.000 claims description 7
- 230000035699 permeability Effects 0.000 claims description 7
- 238000002203 pretreatment Methods 0.000 claims description 7
- 239000004744 fabric Substances 0.000 claims description 6
- 239000002699 waste material Substances 0.000 abstract description 7
- 238000004065 wastewater treatment Methods 0.000 abstract description 6
- 238000004140 cleaning Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract description 3
- 239000001963 growth medium Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000010865 sewage Substances 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000000306 component Substances 0.000 abstract 1
- 238000003912 environmental pollution Methods 0.000 abstract 1
- 230000002349 favourable effect Effects 0.000 abstract 1
- 239000010842 industrial wastewater Substances 0.000 abstract 1
- 238000003825 pressing Methods 0.000 abstract 1
- 238000011268 retreatment Methods 0.000 abstract 1
- 238000012360 testing method Methods 0.000 description 7
- 239000002609 medium Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 235000015097 nutrients Nutrition 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000008399 tap water Substances 0.000 description 4
- 235000020679 tap water Nutrition 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 244000144977 poultry Species 0.000 description 3
- 239000000654 additive Substances 0.000 description 2
- 230000031018 biological processes and functions Effects 0.000 description 2
- 238000012258 culturing Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000012262 fermentative production Methods 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 238000011081 inoculation Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000009418 renovation Methods 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002155 anti-virotic effect Effects 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229930000044 secondary metabolite Natural products 0.000 description 1
- 238000011218 seed culture Methods 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 230000001228 trophic effect Effects 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
Abstract
The invention provides a cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide. The method comprises the following steps: filter-pressing a three-stage fermentation liquor of Streptomyces actuosus, controlling the content of filter solid substances, and taking a filter liquor and a tank body cleaning solution as the fermentation wastewater; treating the fermentation wastewater, and discharging primary sludge to a sludge tank; sending primary treatment wastewater into an MBR (membrane biochemical reaction) tank for secondary treatment; controlling the sludge concentration in the MBR tank; dehydrating the sludge in the sludge tank, and sending water of dehydration back to the MBR tank for retreatment; storing secondary treatment wastewater; and adding a corresponding percentage of culture medium component into the secondary treatment wastewater which is then used for three-stage fermentation of next batch of nosiheptide. On the premise of not influencing the quality of nosiheptide, the problems of high industrial wastewater treatment cost, serious water resource waste and the like of nosiheptide are solved, environmental pollution is avoided, a strict sewage treatment process required for directly discharged waste water is eliminated, the production cost is greatly lowered, and favorable economical and environmental benefits are shown.
Description
Technical field
The invention belongs to the antibiotic fermentation waste water processing technology field, the circulation utilization method that relates to the tank body scavenging solutions such as a kind of nosiheptide fermentation waste water and seeding tank, fermentor tank, pre-treatment tank, these waste water are back to the nosiheptide three grade fermemtation after treatment, are specifically related to fermentation waste water circulation utilization method in a kind of nosiheptide industrial production.
Background technology
Nosiheptide is a kind of novel fodder additives, not only can promote growth of animals or poultry, improve feed efficiency, but also have be difficult for producing resistance, noresidue, little to environmental influence, to characteristics such as person poultry safeties, meet the requirement of green safety fodder additives fully.As antivirus somatotropic agent, it can not only be widely used in poultry industry, can also be widely used in water industry.At present, domestic nosiheptide main manufacturer is Gansu remittance energy company, produces about 30000 ton of 1% Nosiheptide premixed agent per year.
Nosiheptide be by S.actuosus (
Streptomyces actuosus) a kind of secondary metabolite of producing through liquid submerged fermentation, present stage fermentation level about 14000U/ml, produce 5.0 tons of waste water and calculate by producing 1 ton of 1% Nosiheptide premixed agent, will produce 150,000 tons of waste water every year.So huge wastewater flow rate directly discharging meeting causes detrimentally affect to environment, present stage all is to make it reach " fermentation class pharmaceutical industry pollution discharge standard " (GB21903-2008) rear discharging through strict sewage treatment process such as biochemistry, hydrolysis usually, but cost consumption is large, cause simultaneously the waste of great lot of water resources, be unfavorable for the development of recycling economy, do not meet Gansu Province and practice " strict water resources " policy requirements.
Summary of the invention
In order to overcome above-mentioned problems of the prior art, the purpose of this invention is to provide fermentation waste water circulation utilization method in a kind of nosiheptide industrial production, after the tank body scavenging solutions such as nosiheptide fermentation waste water and seeding tank, fermentor tank, pre-treatment tank are processed, be back to the nosiheptide three grade fermemtation, when avoiding contaminate environment, reduce cost, save water resources.
For achieving the above object, the technical solution adopted in the present invention is: fermentation waste water circulation utilization method in a kind of nosiheptide industrial production, after the tank body scavenging solutions such as nosiheptide fermentation waste water and seeding tank, fermentor tank, pre-treatment tank are processed, be back to the nosiheptide three grade fermemtation, when avoiding contaminate environment, reduce cost, save water resources, the method is specifically carried out according to the following steps:
Step 1: with the three grade fermemtation liquid of S.actuosus at 5.0～6.0kg/cm
2Eardrum pressure under press filtration, control filter solid content is 2000～3000mg/L, collects filtrate and tank body scavenging solution, gets fermentation waste water;
Step 2: fermentation waste water is pumped into three grades of mechanical accurate filters of deslagging carry out primary treatment, form primary sludge and solid content less than the primary treatment waste water of 600mg/L, primary sludge is disposed to sludge sump; The flow velocity of fermentation waste water is 5～8m in the primary treatment process
3/ h, hydraulic pressure are 0.2～0.5MPa;
Step 3: primary treatment waste water is sent into MBR film biochemical reaction tank carry out secondary treatment, produce secondary sludge; When sludge concentration is less than 12g/L in the MBR film biochemical reaction tank, primary sludge is back in the MBR film biochemical reaction tank, until sludge concentration equals 13g/L in the MBR film biochemical reaction tank, stop primary sludge and reflux, and the secondary sludge that continues in the MBR film biochemical reaction tank to produce is disposed to sludge sump; At this moment, the mud that concentration equals 13g/L in the MBR film biochemical reaction tank carries out secondary treatment with a waste water;
The secondary sludge that is disposed to sludge sump and the rear remaining primary sludge that refluxes are dewatered, and the water of deviating from returns MBR film biochemical reaction tank and processes;
Store the secondary treatment waste water that MBR film biochemical reaction tank forms;
MBR film biochemical reaction tank is selected the supporting plate type flat sheet membrane: film useful area 300m
2, process wastewater flow 150 m
3 /D, volume load 1.8kgCOD/m
3
. D, sludge concentration 12g/L, design sludge loading 0.15kgCOD/kgMLSS
. D, sludge yield 0.13kgMLSS/ remove kgCOD, sludge yield 0.13kgSS/kgCOD
. D, film aeration rate 50m
3Air/m
3Water outlet, clean membrane flux 26LMH, circulation: operation 9min, lax 1min; Initial permeability rate 4.2LMH/kPa, chemical 0.6%NaOCI:1% oxalic acid;
In the time of the secondary treatment waste water that stores need to being used for the nosiheptide three grade fermemtation, add respectively following medium component in the material-compound tank by the weight of the medium component that needs in every liter of secondary treatment waste water: W-Gum 4～8g/L, soybean cake powder 2～5g/L, emulsifying agent 0～0.2g/L, ammonium sulfate 0～2g/L, light calcium carbonate 0～2g/L, sodium sulfate 0～0.5g/L, GPE0～0.4g/L, soya-bean oil 5～40g/L, dipotassium hydrogen phosphate 0～1g/L and yellow soda ash 0～0.3g/L, the pH value of liquid is 6.0～7.0 behind the control interpolation medium component, forms batching; In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h with the batching in the material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
The inventive method has solved the problems such as the high and water resource waste of cost for wastewater treatment that present domestic nosiheptide industry exists is serious, the cleaning waste liquid that the waste water that produces in the nosiheptide industrial production and the tank body in the cleaning product line produce is processed, be back to the nosiheptide fermentation, not only avoided the pollution to environment, and saved the strict sewage treatment process that direct waste discharge need to carry out, greatly reduced production cost, save simultaneously valuable water resources, shown good economy and environment benefit.
Description of drawings
Accompanying drawing 1 is the schema of circulation utilization method of the present invention.
Embodiment
The present invention is described in detail below in conjunction with the drawings and specific embodiments.
The present invention is directed to the problems such as the large and water resource waste of cost for wastewater treatment that present nosiheptide industry exists is serious, the method for the waste water that produces in a kind of recycle nosiheptide industrial production is provided, the reduction cost economizes on resources.The process flow sheet of the method, as shown in Figure 1, specifically carry out according to the following steps:
Step 1: (it is 14000～14500U/ml) to carry out filter press that unit tires, and is specially: with this three grade fermemtation liquid at 5.0～6.0kg/cm with the three grade fermemtation liquid of S.actuosus 180～220h
2Eardrum pressure under, through 300 order filter cloth press filtrations 2～3 hours, control filter solid content was 2000～3000mg/L, after press filtration is finished, clean various tank bodies (comprising the tank bodies such as seeding tank, fermentor tank, pre-treatment tank), collect filtrate and tank body scavenging solution, get fermentation waste water;
Step 2: filter the suspended substance of removing in the fermentation waste water, namely with topping-up pump fermentation waste water is pumped into three grades of mechanical accurate filters of deslagging and carry out primary treatment, this fermentation waste water is processed by 100 μ m one-level accurate filters, 10 μ m secondary accurate filters and 1 μ m secondary accurate filter in three grades of mechanical accurate filters of deslagging successively, form primary sludge and solid content less than the primary treatment waste water of 600mg/L, primary sludge is disposed to sludge sump; The flow rate control of fermentation waste water is 5～8m in the primary treatment process
3/ h, hydraulic pressure control are 0.2～0.5MPa; Every grade of per 2～3h deslagging of strainer once;
Step 3: primary treatment waste water is sent into integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank carry out secondary treatment, produce secondary sludge; When sludge concentration is less than 12g/L in the MBR film biochemical reaction tank, primary sludge is back in the MBR film biochemical reaction tank, until sludge concentration equals 13g/L in the MBR film biochemical reaction tank, stop primary sludge and reflux, and the secondary sludge that continues in the MBR film biochemical reaction tank to produce is disposed to sludge sump; At this moment, the mud that concentration equals 13g/L in the MBR film biochemical reaction tank carries out secondary treatment with a waste water;
The secondary sludge that is disposed to sludge sump and the rear remaining primary sludge that refluxes are dewatered, and the water of deviating from returns MBR film biochemical reaction tank and processes, and the mud after the dehydration forms mud cake, burns this mud cake;
The secondary treatment waste water that MBR film biochemical reaction tank forms pumps into the temporary tank stores for the treatment of solution;
MBR film biochemical reaction tank is selected the supporting plate type flat sheet membrane: film useful area 300m
2, process wastewater flow 150 m
3 /D, volume load 1.8kgCOD/m
3
. D, sludge concentration 12g/L, design sludge loading 0.15kgCOD/kgMLSS
. D, sludge yield 0.13kgMLSS/ remove kgCOD, sludge yield 0.13kgSS/kgCOD
. D, film aeration rate 50m
3(air)/m
3(water outlet), clean membrane flux 26LMH, circulation: operation 9min, lax 1min; Initial permeability rate 4.2LMH/kPa, chemical 0.6%NaOCI:1% oxalic acid.
Mainly utilize biological action and the physics effect of damming of MBR film in the dual-spectrum process, the organism of holding back in the biological reaction tank makes it keep high concentration to be conducive to biochemical reaction; Under aeration condition, utilize the biological action of membrane bioreactor, absorption is also removed part organic substance in the waste water by biological degradation.
In the time of secondary treatment waste water in the temporary tank for the treatment of solution need to being used for the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into material-compound tank, and add respectively following medium component in the material-compound tank by the weight of the medium component that needs in every liter of secondary treatment waste water in the material-compound tank: W-Gum 4～8g/L, soybean cake powder 2～5g/L, emulsifying agent 0～0.2g/L, ammonium sulfate 0～2g/L, light calcium carbonate 0～2g/L, sodium sulfate 0～0.5g/L, bubble enemy (GPE) 0～0.4g/L, soya-bean oil 5～40g/L, dipotassium hydrogen phosphate 0～1g/L and yellow soda ash 0～0.3g/L, add in the control material-compound tank that the pH value of liquid is 6.0～7.0 behind the medium component, form and prepare burden.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h with the batching in the material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
Preferred medium component and adding proportion are: W-Gum 6.43g/L, soybean cake powder 3.43g/L, emulsifying agent 0.05g/L, ammonium sulfate 1.00g/L, light calcium carbonate 0.56g/L, sodium sulfate 0.10g/L, GPE0.037g/L, soya-bean oil 10g/L, dipotassium hydrogen phosphate 0.05g/L and yellow soda ash 0.063g/L, add in the material-compound tank that the pH value of liquid is 6.0～7.0 behind the medium component.
The inventive method is carried out autoclave diaphragm filter press, solid suspended substance physical sepn, MBR membrane biological reaction, sludge treatment to S.actuosus through 180～220 h fermented liquids, in the processing water that MBR film biochemical reaction tank pumps, add medium component again, the nosiheptide three grade fermemtation that is used for next batch, the waste water that is about to last consignment of time fermentation and cleaning generation is used for the next batch fermentation after treatment, through the industrial test proof nosiheptide fermentation titer is had no significant effect.So that in the nosiheptide three grade fermemtation process, the moisture that in fermentative production, evaporates, the whole process non-wastewater discharge, the water resources recovery utilization rate is increased to 66～71%.Use significantly saving water resource of present method, reduce the pressure to environment, the overall application cost is processed and is disposed to environment and decreases, so has good use value in industrial production.
Adopt the inventive method can make the water resources recovery utilization rate in the nosiheptide industrial production be increased to 66～71%, the below is as follows with the single batch of concrete calculation procedure of fermenting process:
Initial amount of water 0.5～0.6m when 1) first order seed is cultivated
3, the about 0.1m of the culturing process loss water yield (mainly evaporating in the atmosphere)
3So cultivating and remaining the first order seed nutrient solution when finishing is 0.4～0.5m
3, first order seed is cultivated qualified rear direct inoculation and is delivered to secondary seed medium.
Initial amount of water 4.5～4.8m when 2) secondary seed is cultivated
3, add the first order seed in the access first class seed pot, the about 0.3m of the culturing process loss water yield (mainly evaporating in the atmosphere)
3So cultivating and remaining the secondary seed nutrient solution when finishing is 4.2～4.5m
3, secondary seed is cultivated qualified rear inoculation and is delivered to the three grade fermemtation substratum.
3) the three grade fermemtation substratum adds water 35m at first
3, middle by 16 tons of fermentor tank feed supplements, pilot process loses about 9～10 m
3So, final about 41～43 m of fermented liquid
3, be delivered to the fermentation liquor pretreatment tank after the three grade fermemtation cultivation is qualified.
4) process need water flushing behind the fermented liquid filter press, every 40m
3Consume tap water 20m
3Flushing, operating process loss 0.5～1.0m
3So, remove the solid content such as fermented liquid mycelium, about 56.4～58.8 m of filtered liquid behind the filter press
3
5) be used for the fermentation batching through the fermented waste fluid behind the filter press after accurate filter oil removal, MBR Membrane Bioreactor for Wastewater Treatment, this process flows into without new tap water, and the about 3～4m of loss in the process
3So the final water yield is 52.4～55.8m
3
The calculating of above-mentioned 5 step water consumptions, process water loss amount, final residual content is as shown in table 1.
Table 1 nosiheptide fermentation whole process water variable quantity abridged table
| Step | The process water amount | The process loss water yield | Final residual content | The surplus water trend |
| First order seed is cultivated | 0.5~0.6m 3 | About 0.1m 3 | 0.4~0.5m 3 | Secondary seed medium |
| Secondary seed is cultivated | 4.1~4.3m 3 | 0.3m 3 | 4.2~4.5m 3 | The three grade fermemtation substratum |
| Three grade fermemtation is cultivated | 51m 3 | 9~10m 3 | 41~43m 3 | Plate-and-frame filter press |
| Filter press | 20m 3 | 0.5~1.0m 3 | 54.4~56.8m 3 | The wastewater treatment and renovation station |
| Wastewater treatment and renovation | 0m 3 | 3~4m 3 | 50.4~53.8m 3 | The fermented liquid material-compound tank |
As shown in Table 1, the initial water total amount of process is 75.6～75.9m
3, recovery total is 50.4～53.8m
3, the rate of recovery is 66%～71%.
Embodiment 1
With the three grade fermemtation liquid of S.actuosus 180～220h at 5.0kg/cm
2Eardrum pressure under, through 300 order filter cloth press filtrations 3 hours, control filter solid content was 2000mg/L, after press filtration is finished, collected filtrate and tank body (being the tank bodies such as seeding tank, fermentor tank, pre-treatment tank) scavenging solution, got fermentation waste water; With topping-up pump fermentation waste water is pumped into three grades of mechanical accurate filters of deslagging and carry out primary treatment, this fermentation waste water is processed by 100 μ m one-level accurate filters, 10 μ m secondary accurate filters and 1 μ m secondary accurate filter in three grades of mechanical accurate filters of deslagging successively, form primary sludge and solid content less than the primary treatment waste water of 600mg/L, primary sludge is disposed to sludge sump; The flow rate control of fermentation waste water is 5m in the primary treatment process
3/ h, hydraulic pressure control are 0.2MPa; Every grade of per 2～3h deslagging of strainer once; Primary treatment waste water is sent into integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank carry out secondary treatment, produce secondary sludge; When sludge concentration is less than 12g/L in the MBR film biochemical reaction tank, primary sludge is back in the MBR film biochemical reaction tank, until sludge concentration equals 13g/L in the MBR film biochemical reaction tank, stop primary sludge and reflux, and the secondary sludge that continues in the MBR film biochemical reaction tank to produce is disposed to sludge sump; At this moment, the mud that concentration equals 13g/L in the MBR film biochemical reaction tank carries out secondary treatment with a waste water; The secondary sludge that is disposed to sludge sump and the rear remaining primary sludge that refluxes are dewatered, and the water of deviating from returns MBR film biochemical reaction tank and processes, burns the mud after dewatering; The secondary treatment waste water that MBR film biochemical reaction tank forms pumps into the temporary tank stores for the treatment of solution; MBR film biochemical reaction tank is selected the supporting plate type flat sheet membrane: film useful area 300m
2, process wastewater flow 150 m
3 /D, volume load 1.8kgCOD/m
3
. D, sludge concentration 12g/L, design sludge loading 0.15kgCOD/kgMLSS
. D, sludge yield 0.13kgMLSS/ remove kgCOD, sludge yield 0.13kgSS/kgCOD
. D, film aeration rate 50m
3(air)/m
3(water outlet), clean membrane flux 26LMH, circulation: operation 9min, lax 1min; Initial permeability rate 4.2LMH/kPa, chemical 0.6%NaOCI:1% oxalic acid.
In the time of secondary treatment waste water in the temporary tank for the treatment of solution need to being used for the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into material-compound tank, and add respectively following medium component in the material-compound tank by the weight of the medium component that needs in every liter of secondary treatment waste water in the material-compound tank: W-Gum 6.43g/L, soybean cake powder 3.43g/L, emulsifying agent 0.05g/L, ammonium sulfate 1.00g/L, light calcium carbonate 0.56g/L, sodium sulfate 0.10g/L, GPE0.037g/L, soya-bean oil 10g/L, dipotassium hydrogen phosphate 0.05g/L and yellow soda ash 0.063g/L, the pH value of liquid is 6.0 in the temporary tank for the treatment of solution.Form batching.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h with the batching in the material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
Process and do not process fermentation waste water impact is tired relatively by nosiheptide three grade fermemtation unit
Control group: with the three grade fermemtation substratum of tap water preparation;
Test group 1: three grade fermemtation nutrient solution and the feed supplement liquid of using filter press liquid directly to prepare;
Test group 2: adopt the fermentation waste water after embodiment 1 described method is processed.
More than 3 every group of tests are parallel, revision test 3 times.
Except preparation fermention medium water such as embodiment 1 conceptual design, other is all identical such as first order seed substratum water, secondary seed medium water, feed supplement tank water, first order seed culture medium prescription, secondary seed medium prescription, supplemented medium kind and prescription, proportioning process, fermentating controling process condition, fermented liquid aftertreatment technology condition; The used identical 50m of tank body parameter that is
3Fermentor tank.
Control group tap water three grade fermemtation based formulas, except emulsifying agent 0.10g/L and GPE0.05g/L, all the other compositions are all identical, and test group 1 and test group 2 are except the three grade fermemtation nutrient solution of directly preparing with filter press liquid, except except emulsifying agent 0.03g/L and GPE0.03g/L, all the other compositions are all identical.
(annotate: emulsifying agent only plays and disperses vegetables oil effect, GPE also only to play fermenting process elimination foaming, and two kinds of compositions can not lost the comparative advantages with preferred culture medium prescription and control group all without trophic function.）
Test-results is as shown in table 2:
Fermentation waste water is processed and do not processed to table 2 on the relatively (unit: U/ml) of impact of tiring of nosiheptide three grade fermemtation unit
By as seen from Table 2, the untreated fermented liquid after the direct press filtration of sheet frame is compared the impact of tiring with control group comparatively obvious, and the waste water after art breading of the present invention has no significant effect S.actuosus fermentative production nosiheptide.Illustrate and adopt art breading secondary fermentation waste water energy of the present invention to be used for the nosiheptide three grade fermemtation, on the quality of nosiheptide without impact, and saving water resource.
Embodiment 2
With the three grade fermemtation liquid of S.actuosus 180～220h at 6.0kg/cm
2Eardrum pressure under, through 300 order filter cloth press filtrations 2 hours, control filter solid content was 3000mg/L, after press filtration is finished, filter residue is used for the product subsequent production, and collected filtrate and tank body (comprising the tank bodies such as seeding tank, fermentor tank, pre-treatment tank) scavenging solution gets fermentation waste water; With topping-up pump fermentation waste water is pumped into three grades of mechanical accurate filters of deslagging and carry out primary treatment, this fermentation waste water is processed by 100 μ m one-level accurate filters, 10 μ m secondary accurate filters and 1 μ m secondary accurate filter in three grades of mechanical accurate filters of deslagging successively, form primary sludge and solid content less than the primary treatment waste water of 600mg/L, primary sludge is disposed to sludge sump; The flow rate control of fermentation waste water is 8m in the primary treatment process
3/ h, hydraulic pressure control are 0.5MPa; Every grade of per 2～3h deslagging of strainer once; Primary treatment waste water is sent into integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank carry out secondary treatment, produce secondary sludge; When sludge concentration is less than 12g/L in the MBR film biochemical reaction tank, primary sludge is back in the MBR film biochemical reaction tank, until sludge concentration equals 13g/L in the MBR film biochemical reaction tank, stop primary sludge and reflux, and the secondary sludge that continues in the MBR film biochemical reaction tank to produce is disposed to sludge sump; At this moment, the mud that concentration equals 13g/L in the MBR film biochemical reaction tank carries out secondary treatment with a waste water; The secondary sludge that is disposed to sludge sump and the rear remaining primary sludge that refluxes are dewatered, and the water of deviating from returns MBR film biochemical reaction tank and processes, burns the mud after dewatering; The secondary treatment waste water that MBR film biochemical reaction tank forms pumps into the temporary tank stores for the treatment of solution; MBR film biochemical reaction tank is selected the supporting plate type flat sheet membrane: film useful area 300m
2, process wastewater flow 150 m
3 /D, volume load 1.8kgCOD/m
3
. D, sludge concentration 12g/L, design sludge loading 0.15kgCOD/kgMLSS
. D, sludge yield 0.13kgMLSS/ remove kgCOD, sludge yield 0.13kgSS/kgCOD
. D, film aeration rate 50m
3(air)/m
3(water outlet), clean membrane flux 26LMH, circulation: operation 9min, lax 1min; Initial permeability rate 4.2LMH/kPa, chemical 0.6%NaOCI:1% oxalic acid.
In the time of secondary treatment waste water in the temporary tank for the treatment of solution need to being used for the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into material-compound tank, and add respectively following medium component by the weight of the medium component that needs in every liter of secondary treatment waste water in the material-compound tank in material-compound tank: the pH value of liquid is 7.0 in W-Gum 4g/L, soybean cake powder 2g/L and the soya-bean oil 5g/L control material-compound tank, forms and prepares burden.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h with the batching in the material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
Embodiment 3
With the three grade fermemtation liquid of S.actuosus 180～220h at 5.5kg/cm
2Eardrum pressure under, through 300 order filter cloth press filtrations 2.5 hours, control filter solid content was 2500mg/L, after press filtration is finished, collected filtrate and tank body (first class seed pot, secondary seed tank, three grade fermemtation tank, fermentation liquor treatment tank) scavenging solution, i.e. fermentation waste water; With topping-up pump fermentation waste water is pumped into three grades of mechanical accurate filters of deslagging and carry out primary treatment, this fermentation waste water is processed by 100 μ m one-level accurate filters, 10 μ m secondary accurate filters and 1 μ m secondary accurate filter in three grades of mechanical accurate filters of deslagging successively, form primary sludge and solid content less than the primary treatment waste water of 600mg/L, primary sludge is disposed to sludge sump; The flow rate control of fermentation waste water is 6.5m in the primary treatment process
3/ h, hydraulic pressure control are 0.35MPa; Every grade of per 2～3h deslagging of strainer once; Primary treatment waste water is sent into integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank carry out secondary treatment, produce secondary sludge; When sludge concentration is less than 12g/L in the MBR film biochemical reaction tank, primary sludge is back in the MBR film biochemical reaction tank, until sludge concentration equals 13g/L in the MBR film biochemical reaction tank, stop primary sludge and reflux, and the secondary sludge that continues in the MBR film biochemical reaction tank to produce is disposed to sludge sump; At this moment, the mud that concentration equals 13g/L in the MBR film biochemical reaction tank carries out secondary treatment with a waste water; The secondary sludge that is disposed to sludge sump and the rear remaining primary sludge that refluxes are dewatered, and the water of deviating from returns MBR film biochemical reaction tank and processes, burns the mud after dewatering; The secondary treatment waste water that MBR film biochemical reaction tank forms pumps into the temporary tank stores for the treatment of solution; MBR film biochemical reaction tank is selected the supporting plate type flat sheet membrane: film useful area 300m
2, process wastewater flow 150 m
3 /D, volume load 1.8kgCOD/m
3
. D, sludge concentration 12g/L, design sludge loading 0.15kgCOD/kgMLSS
. D, sludge yield 0.13kgMLSS/ remove kgCOD, sludge yield 0.13kgSS/kgCOD
. D, film aeration rate 50m
3(air)/m
3(water outlet), clean membrane flux 26LMH, circulation: operation 9min, lax 1min; Initial permeability rate 4.2LMH/kPa, chemical 0.6%NaOCI:1% oxalic acid.
In the time of secondary treatment waste water in the temporary tank for the treatment of solution need to being used for the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into material-compound tank, and add respectively following medium component in the material-compound tank by the weight of the medium component that needs in every liter of secondary treatment waste water in the material-compound tank: W-Gum 8g/L, soybean cake powder 5g/L, emulsifying agent 0.2g/L, ammonium sulfate 2g/L, light calcium carbonate 2g/L, sodium sulfate 0.5g/L, GPE(steeps the enemy) 0.4g/L, soya-bean oil 40g/L, dipotassium hydrogen phosphate 1g/L and yellow soda ash 0.3g/L, the pH value of liquid is 6.5 in the control material-compound tank, forms batching.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h with the batching in the material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
Embodiment 4
With the three grade fermemtation liquid of S.actuosus 180～220h at 5.2kg/cm
2Eardrum pressure under, through 300 order filter cloth press filtrations 2.8 hours, control filter solid content was 2200mg/L, after press filtration is finished, collected filtrate and tank body (first class seed pot, secondary seed tank, three grade fermemtation tank, fermentation liquor treatment tank) scavenging solution, got fermentation waste water; With topping-up pump fermentation waste water is pumped into three grades of mechanical accurate filters of deslagging and carry out primary treatment, this fermentation waste water is processed by 100 μ m one-level accurate filters, 10 μ m secondary accurate filters and 1 μ m secondary accurate filter in three grades of mechanical accurate filters of deslagging successively, form primary sludge and solid content less than the primary treatment waste water of 600mg/L, primary sludge is disposed to sludge sump; The flow rate control of fermentation waste water is 6m in the primary treatment process
3/ h, hydraulic pressure control are 0.3MPa; Every grade of per 2～3h deslagging of strainer once; Primary treatment waste water is sent into integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank carry out secondary treatment, produce secondary sludge; When sludge concentration is less than 12g/L in the MBR film biochemical reaction tank, primary sludge is back in the MBR film biochemical reaction tank, until sludge concentration equals 13g/L in the MBR film biochemical reaction tank, stop primary sludge and reflux, and the secondary sludge that continues in the MBR film biochemical reaction tank to produce is disposed to sludge sump; At this moment, the mud that concentration equals 13g/L in the MBR film biochemical reaction tank carries out secondary treatment with a waste water; The secondary sludge that is disposed to sludge sump and the rear remaining primary sludge that refluxes are dewatered, and the water of deviating from returns MBR film biochemical reaction tank and processes, burns the mud after dewatering; The secondary treatment waste water that MBR film biochemical reaction tank forms pumps into the temporary tank stores for the treatment of solution; MBR film biochemical reaction tank is selected the supporting plate type flat sheet membrane: film useful area 300m
2, process wastewater flow 150 m
3 /D, volume load 1.8kgCOD/m
3
. D, sludge concentration 12g/L, design sludge loading 0.15kgCOD/kgMLSS
. D, sludge yield 0.13kgMLSS/ remove kgCOD, sludge yield 0.13kgSS/kgCOD
. D, film aeration rate 50m
3(air)/m
3(water outlet), clean membrane flux 26LMH, circulation: operation 9min, lax 1min; Initial permeability rate 4.2LMH/kPa, chemical 0.6%NaOCI:1% oxalic acid.
In the time of secondary treatment waste water in the temporary tank for the treatment of solution need to being used for the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into material-compound tank, and add respectively following medium component in the material-compound tank by the weight of the medium component that needs in every liter of secondary treatment waste water in the material-compound tank: W-Gum 5g/L, soybean cake powder 4g/L, emulsifying agent 0.1g/L, ammonium sulfate 0.5g/L, light calcium carbonate 1g/L, sodium sulfate 03g/L, GPE(steeps the enemy) 0.2g/L, soya-bean oil 25g/L, dipotassium hydrogen phosphate 0.5g/L and yellow soda ash 0.15g/L, the pH value of liquid is 6.0 in the control material-compound tank, forms batching.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h with the batching in the material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
Claims (8)
1. fermentation waste water circulation utilization method in the nosiheptide industrial production, after the tank body scavenging solutions such as nosiheptide fermentation waste water and seeding tank, fermentor tank, pre-treatment tank are processed, be back to the nosiheptide three grade fermemtation, when avoiding contaminate environment, reduce cost, save water resources, it is characterized in that the method is specifically carried out according to the following steps:
Step 1: with the three grade fermemtation liquid of S.actuosus at 5.0～6.0kg/cm
2Eardrum pressure under press filtration, control filter solid content is 2000～3000mg/L, collects filtrate and tank body scavenging solution, gets fermentation waste water;
Step 2: fermentation waste water is pumped into three grades of mechanical accurate filters of deslagging carry out primary treatment, form primary sludge and solid content less than the primary treatment waste water of 600mg/L, primary sludge is disposed to sludge sump; The flow velocity of fermentation waste water is 5～8m in the primary treatment process
3/ h, hydraulic pressure are 0.2～0.5MPa;
Step 3: primary treatment waste water is sent into MBR film biochemical reaction tank carry out secondary treatment, produce secondary sludge; When sludge concentration is less than 12g/L in the MBR film biochemical reaction tank, primary sludge is back in the MBR film biochemical reaction tank, until sludge concentration equals 13g/L in the MBR film biochemical reaction tank, stop primary sludge and reflux, and the secondary sludge that continues in the MBR film biochemical reaction tank to produce is disposed to sludge sump; At this moment, the mud that concentration equals 13g/L in the MBR film biochemical reaction tank carries out secondary treatment with a waste water;
The secondary sludge that is disposed to sludge sump and the rear remaining primary sludge that refluxes are dewatered, and the water of deviating from returns MBR film biochemical reaction tank and processes;
Store the secondary treatment waste water that MBR film biochemical reaction tank forms.
2. fermentation waste water circulation utilization method in the nosiheptide industrial production as claimed in claim 1 is characterized in that, the MBR film biochemical reaction tank in the described step 3 is selected the supporting plate type flat sheet membrane: film useful area 300m
2, process wastewater flow 150 m
3 /D, volume load 1.8kgCOD/m
3
. D, sludge concentration 12g/L, design sludge loading 0.15kgCOD/kgMLSS
. D, sludge yield 0.13kgMLSS/ remove kgCOD, sludge yield 0.13kgSS/kgCOD
. D, film aeration rate 50m
3Air/m
3Water outlet, clean membrane flux 26LMH, circulation: operation 9min, lax 1min; Initial permeability rate 4.2LMH/kPa, chemical 0.6%NaOCI:1% oxalic acid.
3. fermentation waste water circulation utilization method in the nosiheptide industrial production as claimed in claim 1 is characterized in that, the three grade fermemtation liquid in the described step 1 is through 300 order filter cloth press filtrations.
4. fermentation waste water circulation utilization method in the nosiheptide industrial production as claimed in claim 1, it is characterized in that, in the described step 2, fermentation waste water is processed by 100 μ m one-level accurate filters, 10 μ m secondary accurate filters and 1 μ m secondary accurate filter in three grades of mechanical accurate filters of deslagging successively.
5. fermentation waste water circulation utilization method in the nosiheptide industrial production as claimed in claim 1 is characterized in that, adopts integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank in the described step 3.
6. fermentation waste water circulation utilization method in the nosiheptide industrial production as claimed in claim 1 is characterized in that, in the described step 3, the mud after the dehydration is burned.
7. fermentation waste water circulation utilization method in the nosiheptide industrial production as claimed in claim 1, it is characterized in that, in the time of the secondary treatment waste water that stores in the step 3 need to being used for the nosiheptide three grade fermemtation, add respectively following medium component in the material-compound tank by the weight of the medium component that needs in every liter of secondary treatment waste water: W-Gum 4～8g/L, soybean cake powder 2～5g/L, emulsifying agent 0～0.2g/L, ammonium sulfate 0～2g/L, light calcium carbonate 0～2g/L, sodium sulfate 0～0.5g/L, GPE0～0.4g/L, soya-bean oil 5～40g/L, dipotassium hydrogen phosphate 0～1g/L and yellow soda ash 0～0.3g/L, the pH value of liquid is 6.0～7.0 behind the control interpolation medium component, forms batching; In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h with the batching in the material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
8. fermentation waste water circulation utilization method in the nosiheptide industrial production as claimed in claim 7, it is characterized in that the adding proportion of medium component is: W-Gum 6.43g/L, soybean cake powder 3.43g/L, emulsifying agent 0.05g/L, ammonium sulfate 1.00g/L, light calcium carbonate 0.56g/L, sodium sulfate 0.10g/L, GPE0.037g/L, soya-bean oil 10g/L, dipotassium hydrogen phosphate 0.05g/L and yellow soda ash 0.063g/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012105269960A CN103011504B (en) | 2012-12-10 | 2012-12-10 | Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012105269960A CN103011504B (en) | 2012-12-10 | 2012-12-10 | Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103011504A true CN103011504A (en) | 2013-04-03 |
| CN103011504B CN103011504B (en) | 2013-12-11 |
Family
ID=47960682
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012105269960A Active CN103011504B (en) | 2012-12-10 | 2012-12-10 | Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103011504B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112279461A (en) * | 2020-10-19 | 2021-01-29 | 沧州冀环威立雅环境服务有限公司 | High-salinity sewage treatment process for hazardous waste industry |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6362599A (en) * | 1986-09-02 | 1988-03-18 | Mitsubishi Electric Corp | Membrane bioreactor |
| CN101700950A (en) * | 2009-05-22 | 2010-05-05 | 黄景忠 | Method for treating high-concentration fermented wastewater |
| CN101885555A (en) * | 2009-05-12 | 2010-11-17 | 江西金达莱环保研发中心有限公司 | Method for treating fermentative pharmaceutical wastewater |
| EP2511375A1 (en) * | 2011-04-13 | 2012-10-17 | Springhill S.A. | High efficiency fermentation process |
-
2012
- 2012-12-10 CN CN2012105269960A patent/CN103011504B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6362599A (en) * | 1986-09-02 | 1988-03-18 | Mitsubishi Electric Corp | Membrane bioreactor |
| CN101885555A (en) * | 2009-05-12 | 2010-11-17 | 江西金达莱环保研发中心有限公司 | Method for treating fermentative pharmaceutical wastewater |
| CN101700950A (en) * | 2009-05-22 | 2010-05-05 | 黄景忠 | Method for treating high-concentration fermented wastewater |
| EP2511375A1 (en) * | 2011-04-13 | 2012-10-17 | Springhill S.A. | High efficiency fermentation process |
Non-Patent Citations (2)
| Title |
|---|
| 孙振龙等: "一体式平片膜生物反应器处理抗生素废水研究", 《工业用水与废水》 * |
| 王志远等: "微型可调ABR-MBR联合工艺处理Vc发酵废水的研究", 《河南科技》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112279461A (en) * | 2020-10-19 | 2021-01-29 | 沧州冀环威立雅环境服务有限公司 | High-salinity sewage treatment process for hazardous waste industry |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103011504B (en) | 2013-12-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102910785B (en) | Treatment method and device for high-concentration organic wastewater | |
| CN103102034B (en) | Deep treatment reuse method for cellulose ethanol production wastewater | |
| CN102249498A (en) | Biochemical treatment method for waste water from small and medium-sized starch factories | |
| CN207537216U (en) | A kind of baffle plate type anaerobic membrane bioreactor system | |
| CN108947118A (en) | A kind of method of citric acid fermentation utilization of wastewater resource | |
| CN103771655B (en) | A kind for the treatment of process of cellulose alcoholic fermentation waste liquid | |
| CN110981099A (en) | Method for producing ethanol by recycling biogas slurry and vinasse clear liquid and reusing | |
| CN101125720A (en) | Synthetic treating process for pulp waste water | |
| CN101830597B (en) | Treatment method of printing and dying wastewater | |
| CN103408201A (en) | Treatment method of industrial wastewater in silicon wafer mortar recovery | |
| CN113213715A (en) | Combined treatment method for fermentation antibiotic production wastewater | |
| CN110066831B (en) | Method for quickly preparing biogas from kitchen waste | |
| CN103708596B (en) | In a kind of white wine wastewater conventional process, strengthening is removed and reclaims the method for nitrogen phosphorus | |
| CN102757153B (en) | Method for treating wastewater generated during production of 12-hydroxy stearic acid | |
| CN102633405B (en) | Treatment method of papermaking black liquor | |
| CN202643504U (en) | Organic solvent desorbed waste water and oil paint waste water treatment device | |
| CN103243123B (en) | A kind of high level transforms the New Cycle technique of potato vinasse | |
| CN208649036U (en) | The wastewater treatment equipment of synchronous carbon and nitrogen removal | |
| CN103011504B (en) | Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide | |
| CN102659260B (en) | Advanced treatment method for effluent of vinasse wastewater or starchiness raw material biochemical engineering wastewater subjected to biochemical treatment | |
| CN105565598B (en) | A kind of integrated treatment and the Application way of cassava grain stillage waste water and industrial sludge | |
| CN103771611B (en) | The solid-liquid separating method of cellulose alcoholic fermentation waste liquid | |
| CN214299762U (en) | Polyester fiber waste water reuse of reclaimed water device | |
| CN205099544U (en) | Food industry sewage treatment system | |
| CN107082488A (en) | The anaerobic membrane bioreactor and its processing method of a kind of effective processing kitchen waste water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide Effective date of registration: 20150417 Granted publication date: 20131211 Pledgee: The Bank of Nanjing Limited by Share Ltd. of Hangzhou city Small and micro businesses franchise branch Pledgor: ZHEJIANG ESIGMA ANIMAL HEALTH CO.,LTD.|GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD.|Hangzhou Esigma Bio-Tech. Co.,Ltd. Registration number: 2015330000019 |
|
| PLDC | Enforcement, change and cancellation of contracts on pledge of patent right or utility model | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 733000 Wuwei Industrial Park, Gansu, No. 1 Patentee after: GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD. Patentee after: ZHEJIANG ESIGMA BIOTECHNOLOGY Co.,Ltd. Address before: 733000 Wuwei Industrial Park, Gansu, No. 1 Patentee before: GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD. Patentee before: ZHEJIANG ESIGMA ANIMAL HEALTH CO.,LTD. |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20170228 Granted publication date: 20131211 Pledgee: The Bank of Nanjing Limited by Share Ltd. of Hangzhou city Small and micro businesses franchise branch Pledgor: ZHEJIANG ESIGMA BIOTECHNOLOGY Co.,Ltd.|GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD. Registration number: 2015330000019 |
|
| PLDC | Enforcement, change and cancellation of contracts on pledge of patent right or utility model | ||
| PM01 | Change of the registration of the contract for pledge of patent right |
Change date: 20170222 Registration number: 2015330000019 Pledgor after: ZHEJIANG ESIGMA BIOTECHNOLOGY Co.,Ltd. Pledgor after: GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD. Pledgor before: ZHEJIANG ESIGMA ANIMAL HEALTH CO.,LTD. Pledgor before: GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD. Pledgor before: Hangzhou Esigma Bio-Tech. Co.,Ltd. |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Cyclic utilization method of fermentation wastewater produced during industrial production of nosiheptide Effective date of registration: 20170303 Granted publication date: 20131211 Pledgee: The Bank of Nanjing Limited by Share Ltd. of Hangzhou city Small and micro businesses franchise branch Pledgor: GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD.|ZHEJIANG ESIGMA BIOTECHNOLOGY Co.,Ltd. Registration number: 2017330000019 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 733000, No. 18 Zamu Road, Industrial Park, Liangzhou District, Wuwei City, Gansu Province Patentee after: Gansu Dabei Agricultural Biotechnology Co.,Ltd. Country or region after: China Patentee after: ZHEJIANG ESIGMA BIOTECHNOLOGY Co.,Ltd. Address before: 733000 No.1 Industrial Park, Wuwei City, Gansu Province Patentee before: GANSU HUINENG BIOLOGICAL ENGINEERING CO.,LTD. Country or region before: China Patentee before: ZHEJIANG ESIGMA BIOTECHNOLOGY Co.,Ltd. |