CN103011504B - 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
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- CN103011504B CN103011504B CN2012105269960A CN201210526996A CN103011504B CN 103011504 B CN103011504 B CN 103011504B CN 2012105269960 A CN2012105269960 A CN 2012105269960A CN 201210526996 A CN201210526996 A CN 201210526996A CN 103011504 B CN103011504 B CN 103011504B
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- 238000000034 method Methods 0.000 title claims abstract description 73
- 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 17
- 230000004151 fermentation Effects 0.000 title abstract description 17
- 125000004122 cyclic group Chemical group 0.000 title abstract 2
- 239000010802 sludge Substances 0.000 claims abstract description 124
- 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 46
- 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
- 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
- 229910019093 NaOCl Inorganic materials 0.000 claims 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 7
- 238000004065 wastewater treatment Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 3
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- 239000008399 tap water Substances 0.000 description 4
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- Activated Sludge Processes (AREA)
- Separation Using Semi-Permeable Membranes (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 Hui Neng company, produces approximately 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 in the 14000U/ml left and right, 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 discharge meeting causes detrimentally affect to environment, present stage is all through strict sewage treatment process such as biochemistry, hydrolysis, to make it reach " fermentation class pharmaceutical industry pollution discharge standard " to discharge after (GB21903-2008) usually, but cost consumption is large, cause the waste of great lot of water resources simultaneously, 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, reduce costs when avoiding contaminate environment, 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 costs, save water resources, the method is specifically carried out according to the following steps:
Step 1: by the three grade fermemtation liquid of S.actuosus at 5.0～6.0kg/cm
2eardrum pressure under press filtration, controlling the filter solid content is 2000～3000mg/L, collects filtrate and tank body scavenging solution, obtains fermentation waste water;
Step 2: fermentation waste water is pumped into to three grades of mechanical accurate filters of deslagging and carry out primary treatment, form the primary treatment waste water that primary sludge and solid content are less than 600mg/L, primary sludge is disposed to sludge sump; In the primary treatment process, the flow velocity of fermentation waste water is 5～8m
3/ h, hydraulic pressure is 0.2～0.5MPa;
Step 3: primary treatment waste water is sent into to MBR film biochemical reaction tank and carry out secondary treatment, produce secondary sludge; When in MBR film biochemical reaction tank, sludge concentration is less than 12g/L, primary sludge is back in MBR film biochemical reaction tank, until in MBR film biochemical reaction tank, sludge concentration equals 13g/L, stop primary sludge and reflux, and the secondary sludge that continues in MBR film biochemical reaction tank to produce is disposed to sludge sump; Now, the mud that the interior concentration of MBR film biochemical reaction tank equals 13g/L carries out secondary treatment together 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 to MBR film biochemical reaction tank and is processed;
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 stored need to being used for to the nosiheptide three grade fermemtation, by the weight of the medium component needed in every liter of secondary treatment waste water to adding respectively following medium component in 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, GPE0～0.4g/L, soya-bean oil 5～40g/L, dipotassium hydrogen phosphate 0～1g/L and sodium carbonate 0～0.3g/L, after control interpolation medium component, the pH value of liquid is 6.0～7.0, forms batching; In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h by the batching in 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 current 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 cleaning product line are produced 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 valuable water resources simultaneously, shown good economy and environment benefit.
The accompanying drawing explanation
Accompanying drawing 1 is the schema of circulation utilization method of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
The present invention is directed to the problems such as the large and water resource waste of cost for wastewater treatment that current nosiheptide industry exists is serious, the method for the waste water produced in a kind of recycle nosiheptide industrial production is provided, reduce costs, economize on resources.The process flow sheet of the method, as shown in Figure 1, specifically carry out according to the following steps:
Step 1: the three grade fermemtation liquid of S.actuosus 180～220h (it is 14000～14500U/ml that unit tires) is carried out to filter press, be specially: by this three grade fermemtation liquid at 5.0～6.0kg/cm
2eardrum pressure under, through 300 order filter cloth press filtration 2～3 hours, controlling the filter solid content was 2000～3000mg/L, after press filtration completes, clean various tank bodies (comprising the tank bodies such as seeding tank, fermentor tank, pre-treatment tank), collect filtrate and tank body scavenging solution, obtain fermentation waste water;
Step 2: filter the suspended substance of removing in fermentation waste water, with topping-up pump, fermentation waste water is pumped into to 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 successively in three grades of mechanical accurate filters of deslagging, form the primary treatment waste water that primary sludge and solid content are less than 600mg/L, primary sludge is disposed to sludge sump; In the primary treatment process, the flow rate control of fermentation waste water is 5～8m
3/ h, hydraulic pressure control is 0.2～0.5MPa; Every grade of every 2～3h deslagging of strainer once;
Step 3: primary treatment waste water is sent into to integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank and carry out secondary treatment, produce secondary sludge; When in MBR film biochemical reaction tank, sludge concentration is less than 12g/L, primary sludge is back in MBR film biochemical reaction tank, until in MBR film biochemical reaction tank, sludge concentration equals 13g/L, stop primary sludge and reflux, and the secondary sludge that continues in MBR film biochemical reaction tank to produce is disposed to sludge sump; Now, the mud that the interior concentration of MBR film biochemical reaction tank equals 13g/L carries out secondary treatment together 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 to MBR film biochemical reaction tank and is processed, and the mud after 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 dual-spectrum process, the organism of holding back in 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 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 to the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into to material-compound tank, and by the weight of the medium component needed in every liter of secondary treatment waste water in material-compound tank to adding respectively following medium component in 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 sodium carbonate 0～0.3g/L, control in material-compound tank that to add the pH value of liquid after medium component be 6.0～7.0, form batching.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h by the batching in 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 sodium carbonate 0.063g/L, adding the pH value of liquid after medium component in material-compound tank is 6.0～7.0.
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, add medium component in the processing water pumped at MBR film biochemical reaction tank again, nosiheptide three grade fermemtation for next batch, be about to last consignment of time fermentation and the clean waste water produced after treatment for the next batch fermentation, through the industrial test proof, the nosiheptide fermentation titer had no significant effect.Make in nosiheptide three grade fermemtation process, the moisture evaporated in fermentative production, the whole process non-wastewater discharge, the water resources recovery utilization rate is increased to 66～71%.The remarkable saving water resource of application present method, reduce the pressure to environment, and 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%, below 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 atmosphere)
3therefore cultivating residue first order seed nutrient solution while 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 atmosphere)
3therefore cultivating residue secondary seed nutrient solution while 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 approximately 9～10 m
3therefore final fermented liquid is 41～43 m approximately
3, after the three grade fermemtation cultivation is qualified, be delivered to the fermentation liquor pretreatment tank.
4) after the fermented liquid filter press, the process need water rinses, every 40m
3consume tap water 20m
3rinse operating process loss 0.5～1.0m
3therefore, remove the solid content such as fermented liquid mycelium, about 56.4～58.8 m of filtered liquid after filter press
3.
5) through the fermented waste fluid after filter press after accurate filter oil removal, MBR Membrane Bioreactor for Wastewater Treatment for the batching of fermenting, this process flows into without new tap water, and the about 3～4m of loss in process
3therefore 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
By the three grade fermemtation liquid of S.actuosus 180～220h at 5.0kg/cm
2eardrum pressure under, through 300 order filter cloth press filtration 3 hours, controlling the filter solid content was 2000mg/L, after press filtration completes, collected filtrate and tank body (being the tank bodies such as seeding tank, fermentor tank, pre-treatment tank) scavenging solution, obtained fermentation waste water; With topping-up pump, fermentation waste water is pumped into to 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 successively in three grades of mechanical accurate filters of deslagging, form the primary treatment waste water that primary sludge and solid content are less than 600mg/L, primary sludge is disposed to sludge sump; In the primary treatment process, the flow rate control of fermentation waste water is 5m
3/ h, hydraulic pressure control is 0.2MPa; Every grade of every 2～3h deslagging of strainer once; Primary treatment waste water is sent into to integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank and carry out secondary treatment, produce secondary sludge; When in MBR film biochemical reaction tank, sludge concentration is less than 12g/L, primary sludge is back in MBR film biochemical reaction tank, until in MBR film biochemical reaction tank, sludge concentration equals 13g/L, stop primary sludge and reflux, and the secondary sludge that continues in MBR film biochemical reaction tank to produce is disposed to sludge sump; Now, the mud that the interior concentration of MBR film biochemical reaction tank equals 13g/L carries out secondary treatment together 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 to MBR film biochemical reaction tank and is processed, 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 to the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into to material-compound tank, and by the weight of the medium component needed in every liter of secondary treatment waste water in material-compound tank to adding respectively following medium component in 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 sodium carbonate 0.063g/L, in the temporary tank for the treatment of solution, the pH value of liquid is 6.0.Form batching.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h by the batching in 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 to 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 directly prepared with filter press liquid;
Test group 2: adopt the fermentation waste water after the described method of embodiment 1 is processed.
3 every group of above tests are parallel, revision test 3 times.
Except preparation fermention medium water, as embodiment 1 conceptual design, other is as all identical as first order seed substratum water, secondary seed medium water, feed supplement tank water, first order seed culture medium prescription, secondary seed medium formula, supplemented medium kind and formula, proportioning process, fermentating controling process condition, fermented liquid aftertreatment technology condition; Usedly be the 50m that the tank body parameter is identical
3fermentor tank.
Tap water three grade fermemtation based formulas for control group, 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, all without trophic function, can not lost the comparative advantages with preferred culture medium prescription and control group.）
Test-results is as shown in table 2:
Table 2 is processed and is not processed fermentation waste water nosiheptide three grade fermemtation unit is tired and affects relatively (unit: U/ml)
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 for the nosiheptide three grade fermemtation, on the quality of nosiheptide without impact, and saving water resource.
embodiment 2
By the three grade fermemtation liquid of S.actuosus 180～220h at 6.0kg/cm
2eardrum pressure under, through 300 order filter cloth press filtration 2 hours, controlling the filter solid content was 3000mg/L, after press filtration completes, filter residue is 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, obtain fermentation waste water; With topping-up pump, fermentation waste water is pumped into to 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 successively in three grades of mechanical accurate filters of deslagging, form the primary treatment waste water that primary sludge and solid content are less than 600mg/L, primary sludge is disposed to sludge sump; In the primary treatment process, the flow rate control of fermentation waste water is 8m
3/ h, hydraulic pressure control is 0.5MPa; Every grade of every 2～3h deslagging of strainer once; Primary treatment waste water is sent into to integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank and carry out secondary treatment, produce secondary sludge; When in MBR film biochemical reaction tank, sludge concentration is less than 12g/L, primary sludge is back in MBR film biochemical reaction tank, until in MBR film biochemical reaction tank, sludge concentration equals 13g/L, stop primary sludge and reflux, and the secondary sludge that continues in MBR film biochemical reaction tank to produce is disposed to sludge sump; Now, the mud that the interior concentration of MBR film biochemical reaction tank equals 13g/L carries out secondary treatment together 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 to MBR film biochemical reaction tank and is processed, 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 to the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into to material-compound tank, and add respectively following medium component by the weight of the medium component needed in every liter of secondary treatment waste water in material-compound tank in material-compound tank: the pH value that W-Gum 4g/L, soybean cake powder 2g/L and soya-bean oil 5g/L control liquid in material-compound tank is 7.0, forms and prepares burden.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h by the batching in material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
embodiment 3
By the three grade fermemtation liquid of S.actuosus 180～220h at 5.5kg/cm
2eardrum pressure under, through 300 order filter cloth press filtration 2.5 hours, controlling the filter solid content was 2500mg/L, after press filtration completes, 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 to 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 successively in three grades of mechanical accurate filters of deslagging, form the primary treatment waste water that primary sludge and solid content are less than 600mg/L, primary sludge is disposed to sludge sump; In the primary treatment process, the flow rate control of fermentation waste water is 6.5m
3/ h, hydraulic pressure control is 0.35MPa; Every grade of every 2～3h deslagging of strainer once; Primary treatment waste water is sent into to integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank and carry out secondary treatment, produce secondary sludge; When in MBR film biochemical reaction tank, sludge concentration is less than 12g/L, primary sludge is back in MBR film biochemical reaction tank, until in MBR film biochemical reaction tank, sludge concentration equals 13g/L, stop primary sludge and reflux, and the secondary sludge that continues in MBR film biochemical reaction tank to produce is disposed to sludge sump; Now, the mud that the interior concentration of MBR film biochemical reaction tank equals 13g/L carries out secondary treatment together 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 to MBR film biochemical reaction tank and is processed, 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 to the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into to material-compound tank, and by the weight of the medium component needed in every liter of secondary treatment waste water in material-compound tank to adding respectively following medium component in 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 sodium carbonate 0.3g/L, the pH value of controlling liquid in material-compound tank is 6.5, form batching.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h by the batching in material-compound tank to 2.0 tons of nosiheptide three grade fermemtation process feed supplement tank feed supplements.
embodiment 4
By the three grade fermemtation liquid of S.actuosus 180～220h at 5.2kg/cm
2eardrum pressure under, through 300 order filter cloth press filtration 2.8 hours, controlling the filter solid content was 2200mg/L, after press filtration completes, collected filtrate and tank body (first class seed pot, secondary seed tank, three grade fermemtation tank, fermentation liquor treatment tank) scavenging solution, obtained fermentation waste water; With topping-up pump, fermentation waste water is pumped into to 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 successively in three grades of mechanical accurate filters of deslagging, form the primary treatment waste water that primary sludge and solid content are less than 600mg/L, primary sludge is disposed to sludge sump; In the primary treatment process, the flow rate control of fermentation waste water is 6m
3/ h, hydraulic pressure control is 0.3MPa; Every grade of every 2～3h deslagging of strainer once; Primary treatment waste water is sent into to integral type single reaction vessel intermittent aeration MBR film biochemical reaction tank and carry out secondary treatment, produce secondary sludge; When in MBR film biochemical reaction tank, sludge concentration is less than 12g/L, primary sludge is back in MBR film biochemical reaction tank, until in MBR film biochemical reaction tank, sludge concentration equals 13g/L, stop primary sludge and reflux, and the secondary sludge that continues in MBR film biochemical reaction tank to produce is disposed to sludge sump; Now, the mud that the interior concentration of MBR film biochemical reaction tank equals 13g/L carries out secondary treatment together 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 to MBR film biochemical reaction tank and is processed, 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 to the nosiheptide three grade fermemtation, secondary treatment waste water in the temporary tank for the treatment of solution is sent into to material-compound tank, and by the weight of the medium component needed in every liter of secondary treatment waste water in material-compound tank to adding respectively following medium component in 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 sodium carbonate 0.15g/L, the pH value of controlling liquid in material-compound tank is 6.0, form batching.In 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h by the batching in 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 a nosiheptide industrial production, after the tank body scavenging solution of nosiheptide fermentation waste water and seeding tank, fermentor tank, pre-treatment tank is processed, be back to the nosiheptide three grade fermemtation, when avoiding contaminate environment, reduce costs, save water resources, it is characterized in that, the method is specifically carried out according to the following steps:
Step 1: by the three grade fermemtation liquid of S.actuosus at 5.0～6.0kg/cm
2eardrum pressure under press filtration, controlling the filter solid content is 2000～3000mg/L, collects filtrate and tank body scavenging solution, obtains fermentation waste water;
Step 2: fermentation waste water is pumped into to three grades of mechanical accurate filters of deslagging and carry out primary treatment, form the primary treatment waste water that primary sludge and solid content are less than 600mg/L, primary sludge is disposed to sludge sump; In the primary treatment process, the flow velocity of fermentation waste water is 5～8m
3/ h, hydraulic pressure is 0.2～0.5MPa;
Step 3: primary treatment waste water is sent into to MBR film biochemical reaction tank and carry out secondary treatment, produce secondary sludge; When in MBR film biochemical reaction tank, sludge concentration is less than 12g/L, primary sludge is back in MBR film biochemical reaction tank, until in MBR film biochemical reaction tank, sludge concentration equals 13g/L, stop primary sludge and reflux, and the secondary sludge that continues in MBR film biochemical reaction tank to produce is disposed to sludge sump; Now, the mud that the interior concentration of MBR film biochemical reaction tank equals 13g/L carries out secondary treatment together 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 to MBR film biochemical reaction tank and is processed;
Store the secondary treatment waste water that MBR film biochemical reaction tank forms.
2. fermentation waste water circulation utilization method in nosiheptide industrial production as claimed in claim 1, is characterized in that, the MBR film biochemical reaction tank in 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 0.13kgSS/(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%NaOCl:1% oxalic acid.
3. fermentation waste water circulation utilization method in nosiheptide industrial production as claimed in claim 1, is characterized in that, the three grade fermemtation liquid in described step 1 is through 300 order filter cloth press filtrations.
4. fermentation waste water circulation utilization method in nosiheptide industrial production as claimed in claim 1, it is characterized in that, in 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 successively in three grades of mechanical accurate filters of deslagging.
5. fermentation waste water circulation utilization method in 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 described step 3.
6. fermentation waste water circulation utilization method in nosiheptide industrial production as claimed in claim 1, is characterized in that, in described step 3, the mud after dehydration burned.
7. fermentation waste water circulation utilization method in nosiheptide industrial production as claimed in claim 1, it is characterized in that, in the time of the secondary treatment waste water stored in step 3 need to being used for to the nosiheptide three grade fermemtation, by the weight of the medium component needed in every liter of secondary treatment waste water to adding respectively following medium component in 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, GPE0～0.4g/L, soya-bean oil 5～40g/L, dipotassium hydrogen phosphate 0～1g/L and sodium carbonate 0～0.3g/L, after control interpolation medium component, the pH value of liquid is 6.0～7.0, form batching, in 48～176h of lower batch of nosiheptide three grade fermemtation, every 16 h by the batching in 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 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 sodium carbonate 0.063g/L.
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