CN110357934A - A kind of process reducing kasugarnycin production process sewage quantity - Google Patents
A kind of process reducing kasugarnycin production process sewage quantity Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 131
- 230000008569 process Effects 0.000 title claims abstract description 109
- 239000010865 sewage Substances 0.000 title claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 99
- 239000012528 membrane Substances 0.000 claims abstract description 77
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims abstract description 45
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000000855 fermentation Methods 0.000 claims abstract description 41
- 230000004151 fermentation Effects 0.000 claims abstract description 41
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 38
- 239000000706 filtrate Substances 0.000 claims abstract description 37
- 239000000919 ceramic Substances 0.000 claims abstract description 31
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000001728 nano-filtration Methods 0.000 claims abstract description 29
- 230000020477 pH reduction Effects 0.000 claims abstract description 25
- 235000006408 oxalic acid Nutrition 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 238000002834 transmittance Methods 0.000 claims description 25
- 230000004907 flux Effects 0.000 claims description 21
- 238000003756 stirring Methods 0.000 claims description 21
- 230000003020 moisturizing effect Effects 0.000 claims description 19
- 238000001471 micro-filtration Methods 0.000 claims description 11
- 239000000047 product Substances 0.000 claims description 11
- 239000012141 concentrate Substances 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 9
- 230000003247 decreasing effect Effects 0.000 claims description 7
- 238000010792 warming Methods 0.000 claims description 7
- 239000003814 drug Substances 0.000 claims description 3
- 239000000575 pesticide Substances 0.000 claims description 3
- 229920002678 cellulose Polymers 0.000 claims description 2
- 239000001913 cellulose Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 239000002253 acid Substances 0.000 abstract description 11
- 238000000605 extraction Methods 0.000 abstract description 7
- 238000000926 separation method Methods 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 30
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 12
- 235000019270 ammonium chloride Nutrition 0.000 description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 5
- 238000005342 ion exchange Methods 0.000 description 5
- 239000011347 resin Substances 0.000 description 5
- 229920005989 resin Polymers 0.000 description 5
- 238000011282 treatment Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 3
- 244000068988 Glycine max Species 0.000 description 2
- 235000010469 Glycine max Nutrition 0.000 description 2
- 239000003242 anti bacterial agent Substances 0.000 description 2
- 229940088710 antibiotic agent Drugs 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000000502 dialysis Methods 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 241001088165 Streptomyces microaureus Species 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 230000000855 fungicidal effect Effects 0.000 description 1
- 239000000417 fungicide Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 231100001231 less toxic Toxicity 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000011218 seed culture Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
- C07H1/00—Processes for the preparation of sugar derivatives
- C07H1/06—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
- C07H1/00—Processes for the preparation of sugar derivatives
- C07H1/06—Separation; Purification
- C07H1/08—Separation; Purification from natural products
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
- C07H15/00—Compounds containing hydrocarbon or substituted hydrocarbon radicals directly attached to hetero atoms of saccharide radicals
- C07H15/20—Carbocyclic rings
- C07H15/207—Cyclohexane rings not substituted by nitrogen atoms, e.g. kasugamycins
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Biochemistry (AREA)
- Biotechnology (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Molecular Biology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention relates to a kind of processes for reducing kasugarnycin production process sewage quantity, kasugarnycin fermentation liquid are mixed acidification through oxalic acid and sulfuric acid, ceramic membrane filter after heating after the processing of filtrate active carbon, then carries out decoloration film process, finally enters nanofiltration concentration.Compared with prior art, present invention process process is simple, utilizes oxalic acid and sulfuric acid mixing acidification, reduce cost, using traditional active carbon and novel membrane separating method, the new production process of kasugarnycin separation is designed, production wastewater volume is greatly reduced, also the investment of soda acid is reduced, the problems such as high-ammonia-nitrogen sewage is handled is solved from source, can effectively solve environmental issue caused by high pollution, while technological operation is simpler, extraction cost is reduced, the predicament of enterprise's cost of sewage disposal is solved.
Description
Technical field
The invention belongs to farm antibiotics extractive technique fields, and in particular to a kind of reduction kasugarnycin production process sewage
The process of amount.
Background technique
Kasugarnycin is as a kind of green, less toxic, low-residual farm antibiotics class fungicide, before having good market
Scape, main production process core procedure is resin method separation currently on the market, and the regeneration of production process resin column generates a large amount of high
Soda acid, high ammonia-nitrogen wastewater test the sewage treatment capacity and cost control of enterprise, and it is dirty on the other hand to cause biggish environmental protection
Dye problem.
Membrane separation process is the general designation of the method selectively penetrated using Special Film to certain ingredients in liquid.Often
Membrane separating method has dialysis, electrodialysis, reverse osmosis, ultrafiltration, followed by natural dialysis and liquid film technology.In recent years, film point
It has developed rapidly from technology, obtained a large amount of application in fields such as water and wastewater treatments.Active carbon adsorption technology is used at home
Industrial Wastewater Treatment has the history of many years, gradually becomes one of industrial wastewater second level or the main method of tertiary treatment.It is existing
Have in technology not having and combines the two for reducing kasugarnycin production process sewage quantifier elimination.
Summary of the invention
In order to solve the problems in the existing technology, the present invention provides a kind of reduction biological pesticide kasugarnycin and produced
The process of journey sewage quantity, is combined using Activated carbon separation and membrane separating method, can by the optimization of specific process step
To greatly reduce the yield of sewage, the problems such as improving sewage treatment high ammonia nitrogen, production cost is reduced, is solved at enterprise's sewage
Manage cost predicament.Process of the invention is energy-saving, adheres to Green Development theory, increase manufacturing enterprise productivity effect and
Domestic and international competitiveness is conducive to enhance pharmaceutical manufacturer's sustainable development.
To achieve the above object, the present invention adopts the following technical scheme:
A kind of process reducing kasugarnycin production process sewage quantity, includes its following processing step:
1) fermentation liquid acidification: mixing acidification for kasugarnycin fermentation liquid oxalic acid and sulfuric acid, and being adjusted to pH value is 2 .0-
3.0, it is sufficiently stirred and stands, heat up；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and ceramic membrane filter is then carried out, and collects filtrate；
3) active carbon is handled: being added active carbon in ceramic membrane filtrate, active carbon feed liquid after standing, is squeezed into plate by stir process
Frame is filtered, and collects filtrate, obtained filtrate light transmittance > 55%；
4) decoloration film process: sheet frame filtrate carries out decoloration film process, and decoloration film process terminates, and destainer average transmittance is greater than
75%；
5) nanofiltration is concentrated: the clear liquid that decoloration film process obtains carries out nanofiltration concentration, is down to 1/10 or so to volume, dope list
Position reaches 60000-70000u/L, and nanofiltration concentration terminates.
In the preferred embodiments of the present invention, the process includes its following processing step:
1) fermentation liquid acidification: it is 2 .0-3.0 that kasugarnycin fermentation liquid oxalic acid and sulfuric acid substep, which are adjusted to pH value, sufficiently
It stirs and stands, the fermentation liquid steam after acidification is warming up to 60-65 DEG C；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and then carries out ceramic membrane filter, collects filtrate, in filter process,
Pressure is controlled in 0.25-0.3MPa, and fermentating liquid volume is down to 1/3 or so, and membrane pressure curve has obvious ascendant trend, starts to acidification
Pure water is added in tank, continuous or interval is disposably added, and average moisturizing rate is slightly larger than membrane flux, guarantees that souring tank inner volume exists
Between, 1.2 times or so that total amount is fermentating liquid volume are added in membrane pressure and flux stabilized, pure water, stop moisturizing, to body
To 1/3 or so, filtering terminates product；
3) active carbon is handled: ceramic membrane filtrate temperature is controlled at 35-45 DEG C, and the active carbon of 0.3-0.5% is added by volume, stirs
Processing 2-3h is mixed, stirring is stopped, standing 0.5-1h, active carbon feed liquid is squeezed into sheet frame and is filtered, and filtrate, obtained filtrate are collected
Light transmittance > 55%；
4) decoloration film process: sheet frame filtrate carries out decoloration film process, and membrane pressure is controlled in 0.5-0.7Mpa, is down to 1/5-1/ to volume
10, membrane flux occurs being decreased obviously trend, starts to Clear liquid tank moisturizing, dope unit is less than 500u/L, total to Clear liquid tank moisturizing
Amount is 0.2-0.3 times；Decoloration film process terminates, and destainer average transmittance is greater than 75%；
5) nanofiltration is concentrated: the clear liquid that decoloration film process obtains carries out nanofiltration concentration, and membrane pressure is controlled in 0.5-1.0Mpa, to body
Product is down to 1/10 or so, and dope unit reaches 60000-70000u/L, and nanofiltration concentration terminates.
In the preferred embodiments of the present invention, the process also includes to be used to be made by the product of step 5)
Pesticide grade raw medicine, the processing step of pulvis or aqua.
In the preferred embodiments of the present invention, in step 1), adjustment pH uses solid oxalic acid and mass concentration for 10-
20% sulfuric acid solution liquid.
In the preferred embodiments of the present invention, in step 2, the filtering of microfiltration of ceramic membrane membrane tube, membrane tube model CMM-
200, one of CMM-500.
In the preferred embodiments of the present invention, in step 3), active carbon is the pharmaceutical grade powder of the gloomy company of Jiangxi great Lin
Last active carbon.
In the preferred embodiments of the present invention, in step 4), decoloration film uses my company's hollow cellulose film long, film
Cast CMN-10.
In the preferred embodiments of the present invention, in step 5), between 15-20, light transmittance is greater than concentrate OD280
35%。
Compared with prior art, technique core procedure of the invention is kasugarnycin fermentation liquid through oxalic acid and sulfuric acid mixed acid
Change processing, ceramic membrane filter after heating after the processing of filtrate active carbon, then carry out decoloration film process, finally enter nanofiltration concentration.With
Domestic kasugarnycin production of raw medicine producer, should using strong-acid type cation column adsorbing separation as the comparison of core conventional production process
Invented technology process is simple, using oxalic acid and sulfuric acid mixing acidification, reduces cost, utilizes traditional active carbon and novel film point
From method, the new production process of kasugarnycin separation is designed, production wastewater volume is greatly reduced, also reduces the throwing of soda acid
Enter, solve the problems such as high-ammonia-nitrogen sewage is handled from source, can effectively solve environmental issue caused by high pollution, while technique is grasped
Make simpler, reduces extraction cost, solve enterprise's cost of sewage disposal predicament technical advantage and be embodied in.
The present invention replaces traditional resin method to extract kasugarnycin using active carbon and the method that film combines of decolourizing, and avoids
Resin column parses agent ammonium chloride and the regenerated concentrated acid of resin column, highly basic investment etc., further reduced production cost.
For the present invention on the basis of guaranteeing that concentrate quality index further increases, the sewage quantity of production process is than existing work
Skill reduces 40-45%, and ammonia nitrogen input amount reduces 55-60%, other indices of sewage are all declined.
Specific embodiment
It is explained below substantive distinguishing features of the present invention with example, it is understood that, example is not intended to limit for illustrating
The embodiment of the invention, the scope of the present invention are determined with core content according to claims.
Kasugarnycin fermentation liquid source in following embodiments:
The acquisition of kasugarnycin fermentation liquid: using streptomyces microaureus for producing strains, with low temperature soybean cake powder, soya-bean oil, yeast powder,
The raw materials such as liquid sugar, by three-level seed culture, into level four fermentation, Microbe synthesis kasugarnycin, the fermentation of every batch of kasugarnycin
Liquid 23-25m3, content 8-14g/L.
Embodiment 1
1) fermentation liquid acidification: mixing acidification for kasugarnycin fermentation liquid oxalic acid and sulfuric acid, be adjusted to pH2 .5 or so,
It is sufficiently stirred and stands, by the fermentation liquid after acidification, steam is warming up to 60-65 DEG C；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and ceramic membrane filter is then carried out, and collects filtrate；After booting, beats and follow
Then ring 30min starts to collect clear liquid；In filter process, pressure is controlled in 0 .25-0 .3MPa, and fermentating liquid volume is down to 1/3
Left and right, membrane pressure curve have obvious ascendant trend, start to add pure water into souring tank, and continuous or interval is disposably added, average
Moisturizing rate is slightly larger than membrane flux, guarantees souring tank inner volume between 1/2-1/3, membrane pressure and flux stabilized, pure water are added total
Amount is 1.2 times or so of fermentating liquid volume, stops moisturizing, to volume to 1/3 or so, filtering terminates；
3) active carbon is handled: ceramic clear liquid temperature presses 35 DEG C of temperature of production, by volume the active carbon of addition 0.5%, at stirring
2-3h is managed, stirring is stopped, standing 0.5-1h, active carbon feed liquid is squeezed into sheet frame and is filtered, and filtrate, filtrate light transmittance > are collected
55%；
4) decoloration film process: sheet frame clear liquid carries out decoloration film process, and the control of filter process membrane pressure is dropped in 0.5-0.7Mpa to volume
To 1/5-1/10, membrane flux occurs being decreased obviously trend, starts to Clear liquid tank moisturizing, total amount of water is 0.2-0.3 times, dope list
Position is less than 500u/L, and decoloration film process terminates, and destainer average transmittance is greater than 75%；
5) nanofiltration is concentrated: decoloration clear liquid carries out nanofiltration concentration, and membrane pressure is controlled in 0.5-1.0Mpa, is down to 1/10 to volume
Left and right, dope unit reach 60000-70000u/L, and nanofiltration concentration terminates, and for concentrate OD280 between 15-20, light transmittance is big
In 35%；
6) sewage data and original process are compared as follows shown in table 1 and (calculate by 50-55m3 fermentation liquid).
1 original process of table are compared with the water consumption of the technique of embodiment 1 and ammonia nitrogen amount
From process water and ammonia nitrogen input amount, it is compared in conjunction with production draining data, original process generate sewage volume in 200m3
More than, ammonia nitrogen 500-600mg/L, total ammonia nitrogen is in 100-120kg or so；New process extraction process does not have ion-exchange regenerated aquatic products
Raw, sewage quantity volume drops to 100m3 or so, while being not necessarily to the investment of ammonium chloride and concentrated acid, concentrated base, and total ammonia nitrogen input amount maintains
Fermentation liquid primary quantity 60kg, without new incrementss, test specimen determination data is between 200-300mg/L.
Embodiment 2
1) fermentation liquid acidification: kasugarnycin fermentation liquid oxalic acid and 10-20% sulfuric acid substep are adjusted to pH3.0 or so, sufficiently
It stirs and stands, by the fermentation liquid after acidification, steam is warming up to 60-65 DEG C；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and ceramic membrane filter is then carried out, and collects filtrate；After booting, beats and follow
Then ring 30min starts to collect clear liquid；In filter process, pressure is controlled in 0.25-0.3MPa, and fermentating liquid volume is down to 1/3 left side
The right side, membrane pressure curve have obvious ascendant trend, start to add pure water into souring tank, and continuous or interval is disposably added, average to mend
Water speed rate is slightly larger than membrane flux, guarantees souring tank inner volume between 1/2-1/3, total amount is added in membrane pressure and flux stabilized, pure water
It is 1.2 times or so of fermentating liquid volume, stops moisturizing, to volume to 1/3 or so, filtering terminates；
3) active carbon is handled: 0.3% active carbon, stir process 2- is added at 45 DEG C in ceramic clear liquid temperature control by volume
3h stops stirring, stands 0.5-1h, and active carbon feed liquid is squeezed into sheet frame and is filtered, and collects filtrate, filtrate light transmittance > 55%；
4) decoloration film process: sheet frame clear liquid carries out decoloration film process, and the control of filter process membrane pressure is dropped in 0.5-0.7Mpa to volume
To 1/5-1/10, membrane flux occurs being decreased obviously trend, starts to Clear liquid tank moisturizing, total amount of water is 0.2-0.3 times, dope list
Position is less than 500u/L, and decoloration film process terminates, and destainer average transmittance is greater than 75%；
5) nanofiltration is concentrated: decoloration clear liquid carries out nanofiltration concentration, and membrane pressure is controlled in 0.5-1.0Mpa, is down to 1/10 to volume
Left and right, dope unit reach 60000-70000u/L, and nanofiltration concentration terminates, and for concentrate OD280 between 15-20, light transmittance is big
In 35%；
6) sewage data (are calculated) compared with original process by 50-55m3 fermentation liquid as shown in table 2.
2 original process of table are compared with the water consumption of the technique of embodiment 2 and ammonia nitrogen amount
From process water and ammonia nitrogen input amount, it is compared in conjunction with production draining data, original process generate sewage volume in 200m3
More than, ammonia nitrogen 500-600mg/L, total ammonia nitrogen is in 100-120kg or so；New process extraction process does not have ion-exchange regenerated aquatic products
Raw, sewage quantity volume drops to 100m3 or so, while being not necessarily to the investment of ammonium chloride and concentrated acid, concentrated base, and total ammonia nitrogen input amount maintains
Fermentation liquid primary quantity 60kg, without new incrementss, test specimen determination data is between 200-300mg/L.
Embodiment 3
1) fermentation liquid acidification: kasugarnycin fermentation liquid oxalic acid and 10-20% sulfuric acid substep are adjusted to pH2 .5 or so, filled
Divide and stir and stand, by the fermentation liquid after acidification, steam is warming up to 60-65 DEG C；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and ceramic membrane filter is then carried out, and collects filtrate；After booting, beats and follow
Then ring 30min starts to collect clear liquid；In filter process, pressure is controlled in 0.25-0.3MPa, and fermentating liquid volume is down to 1/3 left side
The right side, membrane pressure curve have obvious ascendant trend, start to add pure water into souring tank, and continuous or interval is disposably added, average to mend
Water speed rate is slightly larger than membrane flux, guarantees souring tank inner volume between 1/2-1/3, total amount is added in membrane pressure and flux stabilized, pure water
It is 1.2 times or so of fermentating liquid volume, stops moisturizing, to volume to 1/3 or so, filtering terminates；
3) active carbon is handled: 0.5% active carbon, stir process 2- is added at 35 DEG C in ceramic clear liquid temperature control by volume
3h stops stirring, stands 0.5-1h, and active carbon feed liquid is squeezed into sheet frame and is filtered, and collects filtrate, filtrate light transmittance > 55%；
4) decoloration film process: sheet frame clear liquid carries out decoloration film process, and the control of filter process membrane pressure is dropped in 0.5-0.7Mpa to volume
To 1/5-1/10, membrane flux occurs being decreased obviously trend, starts to Clear liquid tank moisturizing, total amount of water is 0.2-0.3 times, dope list
Position is less than 500u/L, and decoloration film process terminates, and destainer average transmittance is greater than 75%；
5) nanofiltration is concentrated: decoloration clear liquid carries out nanofiltration concentration, and membrane pressure control is down to 1/10 left side in 0.5-1.0Mpa, to volume
The right side, dope unit reach 60000-70000u/L, and nanofiltration concentration terminates, and between 15-20, light transmittance is greater than concentrate OD280
35%；
6) sewage data (are calculated) compared with original process by 50-55m3 fermentation liquid as shown in table 3.
3 original process of table are compared with the water consumption of the technique of embodiment 3 and ammonia nitrogen amount
From process water and ammonia nitrogen input amount, it is compared in conjunction with production draining data, original process generate sewage volume in 200m3
More than, ammonia nitrogen 500-600mg/L, total ammonia nitrogen is in 100-120kg or so；New process extraction process does not have ion-exchange regenerated aquatic products
Raw, sewage quantity volume drops to 100m3 or so, while being not necessarily to the investment of ammonium chloride and concentrated acid, concentrated base, and total ammonia nitrogen input amount maintains
Fermentation liquid primary quantity 60kg, without new incrementss, test specimen determination data is between 200-300mg/L.
Embodiment 4
1) fermentation liquid acidification: kasugarnycin fermentation liquid oxalic acid and 10-20% sulfuric acid substep are adjusted to pH3.0 or so, sufficiently
It stirs and stands, by the fermentation liquid after acidification, steam is warming up to 60-65 DEG C；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and ceramic membrane filter is then carried out, and collects filtrate；After booting, beats and follow
Then ring 30min starts to collect clear liquid；In filter process, pressure is controlled in 0 .25-0 .3MPa, and fermentating liquid volume is down to 1/3
Left and right, membrane pressure curve have obvious ascendant trend, start to add pure water into souring tank, and continuous or interval is disposably added, average
Moisturizing rate is slightly larger than membrane flux, guarantees souring tank inner volume between 1/2-1/3, membrane pressure and flux stabilized, pure water are added total
Amount is 1.2 times or so of fermentating liquid volume, stops moisturizing, to volume to 1/3 or so, filtering terminates；
3) active carbon is handled: 0.5% active carbon, stir process 2- is added at 35 DEG C in ceramic clear liquid temperature control by volume
3h stops stirring, stands 0.5-1h, and active carbon feed liquid is squeezed into sheet frame and is filtered, and collects filtrate, filtrate light transmittance > 55%；
4) decoloration film process: sheet frame clear liquid carries out decoloration film process, and the control of filter process membrane pressure is dropped in 0.5-0.7Mpa to volume
To 1/5-1/10, membrane flux occurs being decreased obviously trend, and decoloration film process terminates, and destainer average transmittance is greater than 75%, dope
Into lower batch materials 3) processing of step active carbon；
5) nanofiltration is concentrated: decoloration clear liquid carries out nanofiltration concentration, and membrane pressure control is down to 1/10 left side in 0.5-1.0Mpa, to volume
The right side, dope unit reach 60000-70000u/L, and nanofiltration concentration terminates, and between 15-20, light transmittance is greater than concentrate OD280
35%；
6) sewage data (are calculated) compared with original process by 50-55m3 fermentation liquid as shown in table 4.
4 original process of table are compared with the water consumption of the technique of embodiment 4 and ammonia nitrogen amount
From process water and ammonia nitrogen input amount, it is compared in conjunction with production draining data, original process generate sewage volume in 200m3
More than, ammonia nitrogen 500-600mg/L, total ammonia nitrogen is in 100-120kg or so；New process extraction process does not have ion-exchange regenerated aquatic products
Raw, sewage quantity volume drops to 100m3 or so, while being not necessarily to the investment of ammonium chloride and concentrated acid, concentrated base, and total ammonia nitrogen input amount maintains
Fermentation liquid primary quantity 60kg, without new incrementss, test specimen determination data is between 200-300mg/L.
Embodiment 5
1) fermentation liquid acidification: kasugarnycin fermentation liquid oxalic acid and 10-20% sulfuric acid substep are adjusted to pH2 .5 or so, filled
Divide and stir and stand, by the fermentation liquid after acidification, steam is warming up to 60-65 DEG C；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and ceramic membrane filter is then carried out, and collects filtrate；After booting, beats and follow
Then ring 30min starts to collect clear liquid；In filter process, pressure is controlled in 0 .25-0 .3MPa, and fermentating liquid volume is down to 1/3
Left and right, membrane pressure curve have obvious ascendant trend, start to add pure water into souring tank, and continuous or interval is disposably added, average
Moisturizing rate is slightly larger than membrane flux, guarantees souring tank inner volume between 1/2-1/3, membrane pressure and flux stabilized, pure water are added total
Amount is 1.2 times or so of fermentating liquid volume, stops moisturizing, to volume to 1/3 or so, filtering terminates；
3) active carbon is handled: 0.3% active carbon, stir process 2- is added at 45 DEG C in ceramic clear liquid temperature control by volume
3h stops stirring, stands 0.5-1h, and active carbon feed liquid is squeezed into sheet frame and is filtered, and collects filtrate, filtrate light transmittance > 55%；
4) decoloration film process: sheet frame clear liquid carries out decoloration film process, and the control of filter process membrane pressure is dropped in 0.5-0.7Mpa to volume
To 1/5-1/10, membrane flux occurs being decreased obviously trend, and decoloration film process terminates, and destainer average transmittance is greater than 75%, dope
Into lower batch materials 3) processing of step active carbon；
5) nanofiltration is concentrated: decoloration clear liquid carries out nanofiltration concentration, and membrane pressure control is down to 1/10 left side in 0.5-1.0Mpa, to volume
The right side, dope unit reach 60000-70000u/L, and nanofiltration concentration terminates, and between 15-20, light transmittance is greater than concentrate OD280
35%；
6) sewage data (are calculated) compared with original process by 50-55m3 fermentation liquid as shown in table 5.
5 original process of table are compared with the water consumption of the technique of embodiment 5 and ammonia nitrogen amount
From process water and ammonia nitrogen input amount, it is compared in conjunction with production draining data, original process generate sewage volume in 200m3
More than, ammonia nitrogen 500-600mg/L, total ammonia nitrogen is in 100-120kg or so；New process extraction process does not have ion-exchange regenerated aquatic products
Raw, sewage quantity volume drops to 100m3 or so, while being not necessarily to the investment of ammonium chloride and concentrated acid, concentrated base, and total ammonia nitrogen input amount maintains
Fermentation liquid primary quantity 60kg, without new incrementss, test specimen determination data is between 200-300mg/L.
As it can be seen that using process of the invention, it can be ensured that in the base for guaranteeing that concentrate quality index further increases
On plinth, the sewage quantity of production process generally reduces 40-45% than prior art, and ammonia nitrogen input amount reduces 60%, sewage its
His indices all while being declined, and the yield of sewage can be greatly reduced using process of the invention, is improved
The problems such as sewage treatment high ammonia nitrogen.
The above description is merely a specific embodiment, but scope of protection of the present invention is not limited thereto, any
The change or replacement expected without creative work, should be covered by the protection scope of the present invention.Therefore, of the invention
Protection scope should be with protection scope defined by claims.
Claims (8)
1. a kind of process for reducing kasugarnycin production process sewage quantity, which is characterized in that include its following processing step:
1) fermentation liquid acidification: kasugarnycin fermentation liquid oxalic acid and sulfuric acid are mixed into acidification, tune pH value is 2 .0-
3.0, it is sufficiently stirred and stands, heat up；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and ceramic membrane filter is then carried out, and collects filtrate；
3) active carbon is handled: being added active carbon in ceramic membrane filtrate, active carbon feed liquid after standing, is squeezed into plate by stir process
Frame is filtered, and collects filtrate, obtained filtrate light transmittance > 55%；
4) decoloration film process: sheet frame filtrate carries out decoloration film process, and decoloration film process terminates, and destainer average transmittance is greater than
75%；
5) nanofiltration is concentrated: the clear liquid that decoloration film process obtains carries out nanofiltration concentration, is down to 1/10 or so to volume, dope list
Position reaches 60000-70000u/L, and nanofiltration concentration terminates.
2. process according to claim 1, which is characterized in that the process is walked comprising its following technique
It is rapid:
1) fermentation liquid acidification: kasugarnycin fermentation liquid oxalic acid and sulfuric acid are mixed into acidification, tune pH value is 2 .0-
3.0, it is sufficiently stirred and stands, the fermentation liquid steam after acidification is warming up to 60-65 DEG C；
2) microfiltration of ceramic membrane: the control of punishment in advance process temperature is stablized, and then carries out ceramic membrane filter, collects filtrate, in filter process,
Pressure is controlled in 0.25-0.3MPa, and fermentating liquid volume is down to 1/3 or so, and membrane pressure curve has obvious ascendant trend, starts to acidification
Pure water is added in tank, continuous or interval is disposably added, and average moisturizing rate is slightly larger than membrane flux, guarantees that souring tank inner volume exists
Between, 1.2 times or so that total amount is fermentating liquid volume are added in membrane pressure and flux stabilized, pure water, stop moisturizing, to body
To 1/3 or so, filtering terminates product；
3) active carbon is handled: ceramic membrane filtrate temperature is controlled at 35-45 DEG C, and the active carbon of 0.3-0.5% is added by volume, stirs
Processing 2-3h is mixed, stirring is stopped, standing 0.5-1h, active carbon feed liquid is squeezed into sheet frame and is filtered, and filtrate, obtained filtrate are collected
Light transmittance > 55%；
4) decoloration film process: sheet frame filtrate carries out decoloration film process, and membrane pressure is controlled in 0.5-0.7Mpa, is down to 1/5-1/ to volume
10, membrane flux occurs being decreased obviously trend, starts to Clear liquid tank moisturizing, dope unit is less than 500u/L, total to Clear liquid tank moisturizing
Amount is 0.2-0.3 times；Decoloration film process terminates, and destainer average transmittance is greater than 75%；
5) nanofiltration is concentrated: the clear liquid that decoloration film process obtains carries out nanofiltration concentration, and membrane pressure is controlled in 0.5-1.0Mpa, to body
Product is down to 1/10 or so, and dope unit reaches 60000-70000u/L, and nanofiltration concentration terminates.
3. process according to claim 1 or 2, which is characterized in that the process also includes by step 5)
Product for pesticide grade raw medicine, the processing step of pulvis or aqua to be made.
4. process according to claim 2, which is characterized in that in step 1), adjustment pH uses solid oxalic acid and matter
Measure the sulfuric acid solution liquid that concentration is 10-20%.
5. process according to claim 2, which is characterized in that in step 2, the filtering of microfiltration of ceramic membrane membrane tube, membrane tube
One of model CMM-200, CMM-500.
6. process according to claim 2, which is characterized in that in step 3), active carbon is the quiet hair in Jiangxi or Fujian
The wooden pharmaceutical grade Powdered Activated Carbon of the gloomy company of great Lin.
7. process according to claim 2, which is characterized in that in step 4), decoloration film uses hollow cellulose film,
Membrane tube model C MN-10.
8. process according to claim 2, which is characterized in that in step 5), concentrate OD280 between 15-20,
Light transmittance is greater than 35%.
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