CN102616972A - Comprehensive recycling method and device for high-salt-content amino acid waste water - Google Patents
Comprehensive recycling method and device for high-salt-content amino acid waste water Download PDFInfo
- Publication number
- CN102616972A CN102616972A CN2012101120317A CN201210112031A CN102616972A CN 102616972 A CN102616972 A CN 102616972A CN 2012101120317 A CN2012101120317 A CN 2012101120317A CN 201210112031 A CN201210112031 A CN 201210112031A CN 102616972 A CN102616972 A CN 102616972A
- Authority
- CN
- China
- Prior art keywords
- communicated
- amino acid
- vapour
- waste water
- liquid separator
- 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
- 239000002351 wastewater Substances 0.000 title claims abstract description 84
- 150000001413 amino acids Chemical class 0.000 title claims abstract description 55
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000004064 recycling Methods 0.000 title claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000012528 membrane Substances 0.000 claims abstract description 34
- 238000001728 nano-filtration Methods 0.000 claims abstract description 26
- 150000003839 salts Chemical class 0.000 claims abstract description 14
- 229910017053 inorganic salt Inorganic materials 0.000 claims abstract description 13
- 239000000126 substance Substances 0.000 claims abstract description 8
- 239000010815 organic waste Substances 0.000 claims abstract description 5
- 239000012535 impurity Substances 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims description 64
- 229940024606 amino acid Drugs 0.000 claims description 51
- 238000001704 evaporation Methods 0.000 claims description 50
- 230000008020 evaporation Effects 0.000 claims description 48
- 239000011552 falling film Substances 0.000 claims description 41
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 29
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 29
- 239000004571 lime Substances 0.000 claims description 29
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 28
- 238000012545 processing Methods 0.000 claims description 21
- 239000012530 fluid Substances 0.000 claims description 19
- 230000000694 effects Effects 0.000 claims description 18
- 239000007787 solid Substances 0.000 claims description 16
- 239000011780 sodium chloride Substances 0.000 claims description 14
- 230000008676 import Effects 0.000 claims description 12
- 108010011485 Aspartame Proteins 0.000 claims description 10
- IAOZJIPTCAWIRG-QWRGUYRKSA-N aspartame Chemical compound OC(=O)C[C@H](N)C(=O)N[C@H](C(=O)OC)CC1=CC=CC=C1 IAOZJIPTCAWIRG-QWRGUYRKSA-N 0.000 claims description 10
- 239000000605 aspartame Substances 0.000 claims description 10
- 229960003438 aspartame Drugs 0.000 claims description 10
- 235000010357 aspartame Nutrition 0.000 claims description 10
- 239000000843 powder Substances 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 10
- 239000002245 particle Substances 0.000 claims description 9
- CKLJMWTZIZZHCS-UHFFFAOYSA-N D-OH-Asp Natural products OC(=O)C(N)CC(O)=O CKLJMWTZIZZHCS-UHFFFAOYSA-N 0.000 claims description 8
- CKLJMWTZIZZHCS-UWTATZPHSA-N L-Aspartic acid Natural products OC(=O)[C@H](N)CC(O)=O CKLJMWTZIZZHCS-UWTATZPHSA-N 0.000 claims description 8
- CKLJMWTZIZZHCS-REOHCLBHSA-N L-aspartic acid Chemical compound OC(=O)[C@@H](N)CC(O)=O CKLJMWTZIZZHCS-REOHCLBHSA-N 0.000 claims description 8
- 229960005261 aspartic acid Drugs 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 8
- COLNVLDHVKWLRT-UHFFFAOYSA-N phenylalanine Natural products OC(=O)C(N)CC1=CC=CC=C1 COLNVLDHVKWLRT-UHFFFAOYSA-N 0.000 claims description 8
- 239000013618 particulate matter Substances 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 7
- 238000012546 transfer Methods 0.000 claims description 7
- 238000002425 crystallisation Methods 0.000 claims description 6
- 230000008025 crystallization Effects 0.000 claims description 6
- 239000004744 fabric Substances 0.000 claims description 6
- 239000008187 granular material Substances 0.000 claims description 6
- 239000012141 concentrate Substances 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 230000004907 flux Effects 0.000 claims description 3
- 239000004745 nonwoven fabric Substances 0.000 claims description 3
- 239000000243 solution Substances 0.000 description 28
- 239000006200 vaporizer Substances 0.000 description 14
- 238000009835 boiling Methods 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000002699 waste material Substances 0.000 description 5
- 239000012267 brine Substances 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 4
- 239000002826 coolant Substances 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000015784 hyperosmotic salinity response Effects 0.000 description 1
- 235000015073 liquid stocks Nutrition 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 235000019600 saltiness Nutrition 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Images
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a comprehensive recycling method for high-salt-content amino acid waste water. The method comprises the following steps of: (1) removing impurities; (2) separating organic substances from inorganic substances; (3) recycling organic substances and extracting salt; and (4) circularly treating. In the comprehensive recycling method and the device for high-salt-content amino acid waste water, amino acid and inorganic salt are separated by using a nanofiltration membrane, and are recycled respectively, so that the problem of treatment of organic waste water is solved, operation is convenient, the treatment cost is low, and high yield is achieved with small investment.
Description
Technical field
The present invention relates to technical field of waste water processing, especially a kind of comprehensive recovery and treatment method and treatment unit thereof of high saliferous amino acid wastewater.
Background technology
Highly salt containing organic waste water is the difficult problem in the wastewater treatment always, in industries such as oil, chemical industry, food, liquid waste disposal, midbody, extensively exists.Common oxygen consumption anaerobic biological is handled the restriction (general saltiness need be lower than 1%) owing to the bacterium salt tolerance and can't be used, and mainly takes multiple-effect evaporation to handle at present.
The processing cost of multiple-effect evaporation is very high, and organism is difficult to reclaim.A lot of organism at high temperature are prone to take place polymerization, produce foam, cause evaporation normally not carry out.Evaporating concentration process need consume a large amount of living steam always, also needs a large amount of water coolants that secondary steam is cooled off.A large amount of latent heat of low-grade like this secondary steam have been wasted, and have also increased the expense of water coolant.For quadruple effect vaporizer; One ton of water of evaporation approximately need consume 0.35 ton steam in the actual production, and the about 15KW of power consumption is if the steam output of device is 15t/h; The market price of steam is 230 yuan/ton at present; Electricity price for industrial uses be 0.75 yuan/(KW.h), then calculated by 300 7200 hours working dayss in 1 year, the working cost of steam is about 9,910,000/year.The principle of work of conventional vaporizer is to make thermal source with the bright steam of boiler for producing; Being heated to the heating of boiling point continued to solution through interchanger makes the solution explosive evaporatoin produce secondary steam; Moisture content in the solution becomes water vapor and from solution, evaporates and separate, and solution itself is concentrated.The secondary steam that evaporative process produces becomes water of condensation with condensed again, and the thermal energy transfer in the secondary steam is diffused in the water coolant again and causes thermal waste and cooling-water consumption in the air.
Mechanical vapour recompression evaporation (Mechanical Vapor Recompression is called for short MVR) technology can be widely used in chemical industry, pharmacy, the environmental protection industry (epi), solution concentration or crystallization.If adopt mechanical vapour recompression evaporation (MVR) power-saving technology; Required motor power is about 660KW (pressing NaCl); According to the geographic energy consumption index in Jiangsu; Electricity price for industrial uses be 0.75 yuan/(KWh), then the annual required working cost of MVR system be 3,560,000/year, the running cost of common relatively multiple-effect saving is about 6,350,000/year.Can know through above comparison, adopt increasing economic efficiency that the MVR system can highly significant, realize target for energy-saving and emission-reduction.The principle of work of mechanical vapour recompression evaporation (MVR) vaporizer is to utilize compressor to compress the secondary steam of vaporizer generation its pressure and temperature is raise, and makes the vaporizer thermal source then and substitutes bright steam.Realize the utilization again of heat energy in the secondary steam, make the heat energy recycling of vaporizer.As long as a spot of power driven compressor work is provided, do not need bright steam just can make vaporizer heat energy recycling, consecutive evaporation.The MVR vaporizer also is appreciated that and is open type heat pump in thermodynamics.The effect of compressor is not to produce the heat that evaporation needs, but the heat formation heat circulation of upgrading and carrying vaporizer.The MVR vaporizer is a vaporizer technology of new generation, is a kind of new and high technology of energy-conserving and environment-protective.
The centrifugal fans that adopt improve steam enthalpy more in the MVR system at present, and general separate unit can make the steam significant temp improve about 8 ℃, also can use the series connection of two typhoon machines, can obtain the steam significant temp and improve about 16 ℃.And organism such as amino acid can cause the elevation of boiling point of brine waste more, thereby make the MVR system to move or the economy reduction.The amino acid brine waste that is produced with production ASPARTAME POWDER BP/USP device is an example, and amino acid brine waste composition is following: 0.1%～0.2% phenylalanine(Phe); 0.1～0.2%L-aspartic acid; Sodium-chlor 8～9%; PH=6.8-7.5.Waste water has been done the boiling point test, and data are following:
| NaCl concentration % | 8.5 | 10 | 11.9 | 15.1 | 20.97 | 24.8 | 28.92 |
| Atmospheric boiling point ℃ | 101.5 | 102.2 | 102.8 | 103.7 | 105.8 | 108 | 110.2 |
When cycles of concentration was 30 times, boiling point was 111.8 degree, and when cycles of concentration was 40 times, boiling point was 115 degree.
And pure NaCl solution boiling point can check in as follows:
| NaCl concentration % | 6.19 | 11.03 | 14.67 | 17.69 | 20.32 | 25.09 | 28.92 |
| Atmospheric boiling point ℃ | 101 | 102 | 103 | 104 | 105 | 107 | 108 |
Can know by above-mentioned data; Amino acid can cause obvious rising to the boiling point of NaCl solution, and the high more solution boiling point that causes of amino acid concentration is high more, when being concentrated into 40 times, adopts the placed in-line MVR of two-stage blower fan system; Will make effective temperature difference have only 1 ℃, heat exchange can't be carried out.The MVR technology can not be used further to the processing of the higher waste water of this type organic solubility this moment, can only be used for the evaporation concentration of waste water at most.If adopt the placed in-line MVR of force 3 wind machine system, though heat exchange is feasible, energy consumption improves greatly, and the equipment input is bigger, uneconomical being suitable for.Still there is not effective treatment process at present for this type of highly salt containing organic waste water.
Summary of the invention
The technical problem that the present invention will solve is: a processing difficult problem that overcomes salt-containing organic wastewater in the prior art; A kind of comprehensive recovery and treatment method and treatment unit thereof of high saliferous amino acid wastewater are provided; After adopting nanofiltration that waste water solution is handled; Organism is separated with inorganic salt, reduce organism, help the evaporation process of brine waste the ebullioscopic influence of waste water.
The technical solution adopted for the present invention to solve the technical problems is: a kind of comprehensive recovery and treatment method of high saliferous amino acid wastewater is characterized in that having following steps:
1. remove impurity: the particle diameter of removing in the ASPARTAME POWDER BP/USP industry salt-containing organic wastewater through strainer surpasses 1 micron granule foreign;
2. separation of organic substances and inorganics: adopt 8 inches nf membrane; Single membrane flux is at 8～12 cubic metres/hour, pressure 2～4MPa, 20～50 ℃ of temperature; Filter the ASPARTAME POWDER BP/USP industry salt-containing organic wastewater of having removed granule foreign, collect concentrated phase waste water and light waste water mutually respectively;
3. reclaim organism and extract salinity: the concentrated phase waste water of step in is 2. carried out iso-electric point regulate, pH value transfers to separated out phenylalanine(Phe) at 5.0～6.0 o'clock, and took out phenylalanine(Phe), separated out the L-aspartic acid when pH value transfers to 2.7-2.9, and taking-up L-aspartic acid; Adopt mechanical vapour recompression vapo(u)rization system to carry out evaporation concentration the light phase waste water of step in 2. and obtain supersaturated solution; In supersaturated solution, isolate NaCl; After starting, mechanical vapour recompression vapo(u)rization system do not need the external world that thermal source is provided; The secondary steam that system self produces improves heat content as thermal source through the machinery recompression, guarantees raw material evaporation concentration in system;
4. circular treatment: in step is isolated amino acid whose concentrated phase waste water and the waste water of isolating salinity in 3., mend the new high saliferous amino acid wastewater of ASPARTAME POWDER BP/USP industry again by the above-mentioned steps cyclical operation.
Step is talked phase waste water described in 3. and before carrying out the evaporation of mechanical vapour recompression vapo(u)rization system, is carried out preheating earlier.
Adopt the water of condensation of mechanical vapour recompression vapo(u)rization system self that light phase waste water is carried out preliminary preheating; Adopt the non-condensable gas of mechanical vapour recompression vapo(u)rization system self with excess steam light waste water mutually to be carried out preheating once more, temperature is 81～82 ℃ after the preheating of light phase waste water.
Described mechanical vapour recompression vapo(u)rization system adopts negative-pressure operation.
A kind of comprehensive recycling and processing device of high saliferous amino acid wastewater; Comprise and be used for amino acid and the isolating nanofiltration separation of inorganic salt system and the mechanical vapour recompression vapo(u)rization system that is used for the inorganic salt evaporative crystallization; The concentrated phase outlet of described nanofiltration separation system is communicated with the amino acid extraction element; The light phase inorganic salt wastewater outlet of described nanofiltration separation system is communicated with the import of mechanical vapour recompression vapo(u)rization system; The supersaturated solution outlet of described mechanical vapour recompression vapo(u)rization system is provided with equipment for separating liquid from solid, and the liquid exit of described equipment for separating liquid from solid is communicated with the import of nanofiltration separation system, and the solid outlet of equipment for separating liquid from solid is communicated with the salinity collection device.
Concrete; Described nanofiltration separation system comprises successively through the placed in-line original fluid container of pipeline, thick level strainer, accurate filter and nf membrane strainer; The concentrated phase outlet of described nf membrane strainer is through the pipeline connection original fluid container; Be connected with liquid supply device in the import of described original fluid container, the pipeline between original fluid container and the thick level strainer is provided with concentrate pump, and the pipeline between accurate filter and the nf membrane strainer is provided with topping-up pump; Be provided with the whipping appts that waste water is mixed in the tank body of described original fluid container, described whipping appts comprises stirring rake and the drive unit that drives the stirring rake action; Described mechanical vapour recompression vapo(u)rization system comprises that imitating evaporation element, two through the preheating unit, of discharge pipe line UNICOM successively imitates evaporation element and forced circulation evaporation unit; Comprise that also mechanical vapour is recompressed secondary steam compression that vapo(u)rization system produces to be improved and be input to one again behind the heat content and imitate evaporation element and the vapor recompression unit of forced circulation evaporation unit as thermal source, the light outlet mutually of described nf membrane strainer is passed through discharge pipe line and is communicated with preheating unit.
Further; Described one imitates evaporation element comprises that one imitates falling-film evaporator, first vapour liquid separator and the first lime set flash tank; Two imitate evaporation element comprises that two imitate falling-film evaporator, second vapour liquid separator and the second lime set flash tank, and the forced circulation evaporation unit comprises pump feed evaporator, forced circulation pump and the 3rd vapour liquid separator; The lower cover of one effect falling-film evaporator is communicated with the upper inlet of first vapour liquid separator and second vapour liquid separator respectively through pipeline; The lower cover that the bottom concentrated solution outlet of first vapour liquid separator is imitated falling-film evaporator through pipeline and is communicated with; The upper cover that the vapour outlet of first vapour liquid separator and two is imitated falling-film evaporator is communicated with; The lower cover that the second vapour liquid separator bottom concentrated solution outlet is imitated falling-film evaporator through pipeline and two is communicated with; The lower cover of two effect falling-film evaporators imitates the upper cover of falling-film evaporators through second recycle pump with two and the upper cover of pump feed evaporator is communicated with; The upper cover of pump feed evaporator is communicated with the 3rd vapour liquid separator through pipeline; The lower cover of pump feed evaporator connects forced circulation pump, and salt pump is divided into two branch roads, wherein a branch road links to each other with the equipment for separating liquid from solid import with the connection of the 3rd vapour liquid separator middle part, another branch road through adopting in the 3rd vapour liquid separator bottom; The condensation-water drain of one effect falling-film evaporator and pump feed evaporator is communicated with the upper cover of the first lime set flash tank through pipeline; The upper cover that the vapour outlet of the first lime set flash tank and two is imitated falling-film evaporator is communicated with, and the condensation-water drain that the first lime set flash tank and two is imitated falling-film evaporator is communicated with the upper cover of the second lime set flash tank; The vapour outlet of second vapour liquid separator, the 3rd vapour liquid separator and the second lime set flash tank is communicated with the vapor recompression unit, and the unitary vapour outlet of vapor recompression is communicated with the steam inlet of an effect falling-film evaporator and pump feed evaporator.
Further improve filter effect; And realize uninterrupted serialization production; The concentrated phase outlet of the nf membrane strainer of described nanofiltration separation system and the pipeline between the original fluid container are provided with and are used for temporary concentrated phase waste water and extract amino acid whose extractor; Described thick level strainer is a cloth envelop collector; But the non-woven fabrics filter bag that the filtering particle diameter surpasses the particulate matter of micron detachably is installed in the described cloth envelop collector, but described accurate filter adopts the filtering particle diameter to surpass the filter core of the particulate matter of micron, is above nf membrane but described nf membrane strainer adopts molecular weight cut-off.
For improving pre-heat effect; Make full use of the heat energy of mechanical vapour recompression vapo(u)rization system self; Described preheating unit is the two-stage preheating, and plate type preheater is adopted in first step preheating, and the shell-and-tube preheater is adopted in second stage preheating; The condensation-water drain of the second lime set flash tank is communicated with plate type preheater through the lime set pump, and the non-condensable gas and the excess steam of an effect falling-film evaporator and pump feed evaporator are communicated with the shell-and-tube preheater through vacuum pump.
As preferably, described vapor recompression unit is when load adopts the roots blower compressor during less than 5 tons/hour; Load adopts the centrifugal blower compressor during greater than 5 tons/hour.
The invention has the beneficial effects as follows; The comprehensive recovery and treatment method of high saliferous amino acid wastewater of the present invention and treatment unit utilization nf membrane thereof are separated amino acid with inorganic salt; Recycle respectively then, solved a processing difficult problem that contains organic waste water, easy to operate; Processing cost is low, and small investment realizes big output.
Advantage is: the secondary steam that come out from separator (1), improve heat content through compressor, and temperature raises; Remake heating thermal source, carry out heat exchange, need provide few part to give birth to the steam when driving with liquid stock in the vaporizer for vaporizer; System's needed thermal source in service is all settled a dispute by the parties concerned themselves by system, does not need to replenish in addition to give birth to steam, and the electric energy of compressor operating only need be provided; And the consumption of electric energy is far smaller than the consumption of steam energy, and power consumption reduces greatly; (2) zero(ppm) water behind the vaporizer shell side vapor condensation does not need to dispose in addition the condensing surface cooling, has not only practiced thrift cooling circulating water, also can deliver in the preheater in addition raw material is carried out preheating; Not only heat is rationally utilized; The zero(ppm) water that temperature reduces gets into the industrial cycle pond, and as other process water, water resources also obtains reasonable recycle; System operation running cost reduces greatly, the energy saving economy remarkable benefit; (3) whole evaporation separation system volume is less, takes up an area of to lack, and technical process is simple, efficient, energy-conservation.
Adopt mechanical vapour recompression evaporation (MVR) power-saving technology; Required motor power is about 660KW (pressing NaCl); According to the geographic energy consumption index in Jiangsu; Electricity price for industrial uses be 0.75 yuan/(KWh), then the annual required working cost of MVR system be 3,560,000/year, the running cost of common relatively multiple-effect saving is about 6,350,000/year.Can know through above comparison, adopt increasing economic efficiency that the MVR system can highly significant, can help the enterprises implement target for energy-saving and emission-reduction.
Description of drawings
Below in conjunction with accompanying drawing and embodiment the present invention is further specified.
Fig. 1 is the schematic block diagram of first embodiment of the comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;
Fig. 2 is the schematic block diagram of nanofiltration separation system among first embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;
Fig. 3 is the structural representation of nanofiltration separation system among first embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;
Fig. 4 is the schematic block diagram of second embodiment of the comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;
Fig. 5 is the schematic block diagram of nanofiltration separation system among second embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;
Fig. 6 is the structural representation of nanofiltration separation system among second embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;
Fig. 7 is the schematic block diagram of mechanical vapour recompression vapo(u)rization system in the comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;
Fig. 8 is the structural representation of second embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention.
Among the figure: 1. original fluid container, 11. stirring rakes, 12. drive units, 13. extractors, 2. thick grade strainer; 3. accurate filter, 4. the nf membrane strainer 5. one is imitated evaporation element, and 51. 1 imitate falling-film evaporators, 52. first vapour liquid separators; 53. the first lime set flash tank 6. two is imitated evaporation element, 61. 2 imitate falling-film evaporator, 62. second vapour liquid separators; 63. the second lime set flash tank, 7 forced circulation evaporation unit, 71. pump feed evaporators, 72. forced circulation pumps; 73. the 3rd vapour liquid separator, 8. plate type preheater, 9. shell-and-tube preheater, 10. roots blower compressor.
Among Fig. 7 Fig. 8: waste water---
Water of condensation--------
Steam-------
Embodiment
Combine accompanying drawing that the present invention is done further detailed explanation now.These accompanying drawings are the synoptic diagram of simplification, substruction of the present invention only is described in a schematic way, so it only show the formation relevant with the present invention.
The comprehensive recovery and treatment method of high saliferous amino acid wastewater of the present invention has following steps:
1. remove impurity: the particle diameter of removing in the ASPARTAME POWDER BP/USP industry salt-containing organic wastewater through strainer surpasses 1 micron granule foreign;
2. separation of organic substances and inorganics: adopt 8 inches nf membrane; Single membrane flux is at 8～12 cubic metres/hour, pressure 2～4MPa, 20～50 ℃ of temperature; Filter the ASPARTAME POWDER BP/USP industry salt-containing organic wastewater of having removed granule foreign, collect concentrated phase waste water and light waste water mutually respectively;
3. reclaim organism and extract salinity: the concentrated phase waste water of step in is 2. carried out iso-electric point regulate, pH value transfers to separated out phenylalanine(Phe) at 5.0～6.0 o'clock, and took out phenylalanine(Phe), separated out the L-aspartic acid when pH value transfers to 2.7-2.9, and taking-up L-aspartic acid; Adopting mechanical vapour recompression vapo(u)rization system to carry out evaporation concentration the light phase waste water of step in 2. obtains supersaturated solution, in supersaturated solution, isolates NaCl;
4. circular treatment: in step is isolated amino acid whose concentrated phase waste water and the waste water of isolating salinity in 3., mend the new high saliferous amino acid wastewater of ASPARTAME POWDER BP/USP industry again by the above-mentioned steps cyclical operation.
Further, step is talked phase waste water described in 3. and before carrying out the evaporation of mechanical vapour recompression vapo(u)rization system, is carried out preheating earlier.Adopt the water of condensation of mechanical vapour recompression vapo(u)rization system self that light phase waste water is carried out preliminary preheating; Adopt the non-condensable gas of mechanical vapour recompression vapo(u)rization system self with excess steam light waste water mutually to be carried out preheating once more, temperature is 81～82 ℃ after the preheating of light phase waste water.
For cutting down the consumption of energy, described mechanical vapour recompression vapo(u)rization system adopts negative-pressure operation.
First embodiment of the comprehensive recycling and processing device of Fig. 1 Fig. 2 high saliferous amino acid wastewater of the present invention shown in Figure 3; Comprise and be used for amino acid and the isolating nanofiltration separation of inorganic salt system and the mechanical vapour recompression vapo(u)rization system that is used for the inorganic salt evaporative crystallization; The concentrated phase outlet of nanofiltration separation system is communicated with the amino acid extraction element; The light phase inorganic salt wastewater outlet of nanofiltration separation system is communicated with the import of mechanical vapour recompression vapo(u)rization system; The supersaturated solution outlet of mechanical vapour recompression vapo(u)rization system is provided with equipment for separating liquid from solid; The liquid exit of equipment for separating liquid from solid is communicated with the import of nanofiltration separation system, and the solid outlet of equipment for separating liquid from solid is communicated with the salinity collection device.
Shown in Figure 2; The nanofiltration separation system comprises successively through the placed in-line original fluid container of pipeline 1, thick level strainer 2, accurate filter 3 and nf membrane strainer 4; The concentrated phase outlet of nf membrane strainer 4 is through pipeline connection original fluid container 1; Be connected with liquid supply device in the import of original fluid container 1, the pipeline between original fluid container 1 and the thick level strainer 2 is provided with concentrate pump, and the pipeline between accurate filter 3 and the nf membrane strainer 4 is provided with topping-up pump; Be provided with the whipping appts that waste water is mixed in the tank body of original fluid container 1, whipping appts comprises stirring rake 11 and the drive unit 12 that drives the stirring rake action;
Mechanical vapour recompression vapo(u)rization system comprises that imitating evaporation element 5, two through the preheating unit, of discharge pipe line UNICOM successively imitates evaporation element 6 and forced circulation evaporation unit 7; Comprise that also mechanical vapour is recompressed secondary steam compression that vapo(u)rization system produces to be improved and be input to one again behind the heat content and imitate evaporation element 5 and the vapor recompression unit of forced circulation evaporation unit 7 as thermal source, the light outlet mutually of nf membrane strainer 4 is communicated with preheating unit through discharge pipe line.
One imitates evaporation element 5 comprises that one imitates falling-film evaporator 51, first vapour liquid separator 52 and the first lime set flash tank 53; Two imitate evaporation element 6 comprises that two imitate falling-film evaporator 61, second vapour liquid separator 62 and the second lime set flash tank 63, and forced circulation evaporation unit 7 comprises pump feed evaporator 71, forced circulation pump 72 and the 3rd vapour liquid separator 73;
The lower cover of one effect falling-film evaporator 51 is communicated with the upper inlet of first vapour liquid separator 52 and second vapour liquid separator 62 respectively through pipeline; The lower cover that the bottom concentrated solution outlet of first vapour liquid separator 52 is imitated falling-film evaporator 51 through pipeline and is communicated with; The upper cover that the vapour outlet of first vapour liquid separator 52 and two is imitated falling-film evaporator 61 is communicated with; The lower cover that second vapour liquid separator, 62 bottom concentrated solution outlets are imitated falling-film evaporator 61 through pipeline and two is communicated with; The lower cover of two effect falling-film evaporators 61 imitates the upper cover of falling-film evaporators 61 through second recycle pump with two and the upper cover of pump feed evaporator 71 is communicated with; The upper cover of pump feed evaporator 71 is communicated with the 3rd vapour liquid separator 73 through pipeline; The lower cover of pump feed evaporator 71 connects forced circulation pump 72, the three vapour liquid separators 73 bottoms, and salt pump is divided into two branch roads, wherein a branch road links to each other with the equipment for separating liquid from solid import with the connection of the 3rd vapour liquid separator 73 middle parts, another branch road through adopting; The condensation-water drain of one effect falling-film evaporator 51 and pump feed evaporator 71 is communicated with the upper cover of the first lime set flash tank 53 through pipeline; The upper cover that the vapour outlet of the first lime set flash tank 53 and two is imitated falling-film evaporator 61 is communicated with, and the condensation-water drain that the first lime set flash tank 53 and two is imitated falling-film evaporator 61 is communicated with the upper cover of the second lime set flash tank 63; The vapour outlet of second vapour liquid separator 62, the 3rd vapour liquid separator 73 and the second lime set flash tank 63 is communicated with the vapor recompression unit, the unitary vapour outlet of vapor recompression be communicated with one imitate falling-film evaporator 51 and pump feed evaporator 71 steam inlet.
Fig. 4 Fig. 5 is shown in Figure 6 to be second embodiment of the present invention, and the difference of first embodiment is: the concentrated phase outlet of the nf membrane strainer 4 of nanofiltration separation system and the pipeline between the original fluid container 1 are provided with and are used for temporary concentrated phase waste water and extract amino acid whose extractor 13.Be convenient to realize uninterrupted cyclical operation.
Fig. 7 is shown in Figure 8; Preheating unit is the two-stage preheating; Plate type preheater 8 is adopted in first step preheating; Second stage preheating adopts the condensation-water drain of shell-and-tube preheater 9, the second lime set flash tanks 63 to be communicated with shell-and-tube preheater 9 through vacuum pump through non-condensable gas and the excess steam that the lime set pump is communicated with plate type preheater 8, one effect falling-film evaporators 51 and pump feed evaporator 71.
The vapor recompression unit adopts roots blower compressor 10 when loading less than 5 tons/hour, when loading greater than 5 tons/hour, adopt the centrifugal blower compressor.
The present invention is set forth in wastewater treatment below in conjunction with concrete: choose contain that organic substrate concentration is 2.85%, NaCl concentration is 8.5% amino acid solution 5000L, at first carries out coarse filtration and smart filter, removes particulate matter; Adopt nf membrane to filter then, NaCl and water molecules can see through nf membrane and obtain light phase, and amino acid is because molecule is trapped within concentrated phase more greatly; Thereby realized that material concentrates, after filtering through nf membrane, can get light phase 4500L at last; Its organic concentration reduces to 0.3%; And it is almost constant to contain NaCl concentration, and the solution of light phase also directly carried out evaporative crystallization and obtained salinity this moment, and the concentrated phase organic concentration becomes 25.8%.Because of amino acid can be separated out when the suitable pH value; The solution of concentrated phase is regulated different pH values makes phenylalanine(Phe) and L-aspartic acid separate out the back utilization respectively; The organic concentration of last mother liquor is lower than at 5% o'clock; Can get into nf membrane and filter the concentrated organism of continuation, or get back to the new solution of head tank 1 adding, realize uninterrupted circular treatment again through above-mentioned steps.The solution of other different concns can adopt aforesaid method to carry out separating of amino acid and inorganic salt, repeats no more at this.
The solution of light phase adopts mechanical vapour recompression vapo(u)rization system to carry out evaporative crystallization, concentrates step by step, up to the supersaturated solution that forms NaCl; Carry out solid-liquid separation again, solid is the NaCl crystal, and the amino acid concentration in the liquid also raises; Can return above-mentioned raw materials jar 1 circulates; For making the vapo(u)rization system heat exchange feasible, generally need the control organic content in 3%, it is in 9 degree that experiment obtains the elevation of boiling point.When mechanical vapour recompression vapo(u)rization system was concentrated to organic concentration 3%, the liquid concentrator with 10% went through the nanofiltration separation system, got back to mechanical vapour recompression vapo(u)rization system after making organic concentration reduce to 0.3%.
The method that adopts nanofiltration to combine with mechanical vapour recompression evaporation; Detect evaporating the resulting product in back, shown in the detected result following table 1, test-results shows that zero(ppm) water COD part appearance numerical value is higher; Be since in the experiment liquid level too high or seethed with excitement and acutely cause; Can avoid in the actual production, bigger device can be so that zero(ppm) water COD maintains below 500, and this water adds the water quality requirement that sterilization just can reach cooling circulating water with common biochemical treatment; Thereby, realize recycling economy as circulating cooling make-up water usefulness.
Table 1 zero(ppm) water COD (index of organic content)
With above-mentioned foundation desirable embodiment of the present invention is enlightenment, and through above-mentioned description, the related work personnel can carry out various change and modification fully in the scope that does not depart from this invention technological thought.The technical scope of this invention is not limited to the content on the specification sheets, must confirm its technical scope according to the claim scope.
Claims (10)
1. the comprehensive recovery and treatment method of a high saliferous amino acid wastewater is characterized in that having following steps:
1. remove impurity: the particle diameter of removing in the ASPARTAME POWDER BP/USP industry salt-containing organic wastewater through strainer surpasses 1 micron granule foreign;
2. separation of organic substances and inorganics: adopt 8 inches nf membrane; Single membrane flux is at 8～12 cubic metres/hour, pressure 2～4MPa, 20～50 ℃ of temperature; Filter the ASPARTAME POWDER BP/USP industry salt-containing organic wastewater of having removed granule foreign, collect concentrated phase waste water and light waste water mutually respectively;
3. reclaim organism and extract salinity: the concentrated phase waste water of step in is 2. carried out iso-electric point regulate, pH value transfers to separated out phenylalanine(Phe) at 5.0～6.0 o'clock, and took out phenylalanine(Phe), separated out the L-aspartic acid when pH value transfers to 2.7-2.9, and taking-up L-aspartic acid; Adopting mechanical vapour recompression vapo(u)rization system to carry out evaporation concentration the light phase waste water of step in 2. obtains supersaturated solution, in supersaturated solution, isolates NaCl;
4. circular treatment: in step is isolated amino acid whose concentrated phase waste water and the waste water of isolating salinity in 3., mend the new high saliferous amino acid wastewater of ASPARTAME POWDER BP/USP industry again by the above-mentioned steps cyclical operation.
2. the comprehensive recovery and treatment method of high saliferous amino acid wastewater as claimed in claim 1 is characterized in that: step is talked phase waste water described in 3. and before carrying out the evaporation of mechanical vapour recompression vapo(u)rization system, is carried out preheating earlier.
3. the comprehensive recovery and treatment method of high saliferous amino acid wastewater as claimed in claim 2; It is characterized in that: adopt the water of condensation of mechanical vapour recompression vapo(u)rization system self that light phase waste water is carried out preliminary preheating; Adopt the non-condensable gas of mechanical vapour recompression vapo(u)rization system self with excess steam light waste water mutually to be carried out preheating once more, temperature is 81～82 ℃ after the preheating of light phase waste water.
4. the comprehensive recovery and treatment method of high saliferous amino acid wastewater as claimed in claim 1 is characterized in that: described mechanical vapour recompression vapo(u)rization system adopts negative-pressure operation.
5. the comprehensive recycling and processing device of a high saliferous amino acid wastewater; It is characterized in that: comprise being used for amino acid and the isolating nanofiltration separation of inorganic salt system and the mechanical vapour recompression vapo(u)rization system that is used for the inorganic salt evaporative crystallization; The concentrated phase outlet of described nanofiltration separation system is communicated with the amino acid extraction element; The light phase inorganic salt wastewater outlet of described nanofiltration separation system is communicated with the import of mechanical vapour recompression vapo(u)rization system; The supersaturated solution outlet of described mechanical vapour recompression vapo(u)rization system is provided with equipment for separating liquid from solid; The liquid exit of described equipment for separating liquid from solid is communicated with the import of nanofiltration separation system, and the solid outlet of equipment for separating liquid from solid is communicated with the salinity collection device.
6. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 5; It is characterized in that: described nanofiltration separation system comprises successively through the placed in-line original fluid container of pipeline (1), thick level strainer (2), accurate filter (3) and nf membrane strainer (4); The concentrated phase outlet of described nf membrane strainer (4) is through pipeline connection original fluid container (1); Be connected with liquid supply device in the import of described original fluid container (1); Pipeline between original fluid container (1) and the thick level strainer (2) is provided with concentrate pump; Pipeline between accurate filter (3) and the nf membrane strainer (4) is provided with topping-up pump, is provided with the whipping appts that waste water is mixed in the tank body of described original fluid container (1), and described whipping appts comprises stirring rake (11) and drives the drive unit (12) of stirring rake (11) action;
Described mechanical vapour recompression vapo(u)rization system comprises that imitating evaporation element (5), two through the preheating unit, of discharge pipe line UNICOM successively imitates evaporation element (6) and forced circulation evaporation unit (7); Comprise that also mechanical vapour is recompressed secondary steam compression that vapo(u)rization system produces to be improved and be input to one again behind the heat content and imitate evaporation element (5) and forced circulation evaporation unit (7) the vapor recompression unit as thermal source, the light outlet mutually of described nf membrane strainer (4) is passed through discharge pipe line and is communicated with preheating unit.
7. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 6; It is characterized in that: described one imitates evaporation element (5) comprises that one imitates falling-film evaporator (51), first vapour liquid separator (52) and the first lime set flash tank (53); Two imitate evaporation element (6) comprises that two imitate falling-film evaporator (61), second vapour liquid separator (62) and the second lime set flash tank (63), and forced circulation evaporation unit (7) comprise pump feed evaporator (71), forced circulation pump (72) and the 3rd vapour liquid separator (73);
The lower cover of one effect falling-film evaporator (51) is communicated with the upper inlet of first vapour liquid separator (52) and second vapour liquid separator (62) respectively through pipeline; The lower cover that the bottom concentrated solution outlet of first vapour liquid separator (52) is imitated falling-film evaporator (51) through pipeline and is communicated with; The upper cover that the vapour outlet of first vapour liquid separator (52) and two is imitated falling-film evaporator (61) is communicated with; The lower cover that second vapour liquid separator (62) bottom concentrated solution outlet is imitated falling-film evaporator (61) through pipeline and two is communicated with; The lower cover of two effect falling-film evaporators (61) imitates the upper cover of falling-film evaporators (61) through second recycle pump with two and the upper cover of pump feed evaporator (71) is communicated with; The upper cover of pump feed evaporator (71) is communicated with the 3rd vapour liquid separator (73) through pipeline; The lower cover of pump feed evaporator (71) connects forced circulation pump (72), and salt pump is divided into two branch roads, wherein a branch road links to each other with the equipment for separating liquid from solid import with the connection of the 3rd vapour liquid separator (73) middle part, another branch road through adopting in the 3rd vapour liquid separator (73) bottom;
The condensation-water drain of one effect falling-film evaporator (51) and pump feed evaporator (71) is communicated with the upper cover of the first lime set flash tank (53) through pipeline; The upper cover that the vapour outlet of the first lime set flash tank (53) and two is imitated falling-film evaporator (61) is communicated with, and the condensation-water drain that the first lime set flash tank (53) and two is imitated falling-film evaporator (61) is communicated with the upper cover of the second lime set flash tank (63);
The vapour outlet of second vapour liquid separator (62), the 3rd vapour liquid separator (73) and the second lime set flash tank (63) is communicated with the vapor recompression unit, and the unitary vapour outlet of vapor recompression is communicated with the steam inlet of an effect falling-film evaporator (51) and pump feed evaporator (71).
8. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 6; It is characterized in that: the concentrated phase outlet of the nf membrane strainer (4) of described nanofiltration separation system is provided with the pipeline between the original fluid container (1) and is used for keeping in concentrated phase waste water and extracting amino acid whose extractor (13); Described thick level strainer (2) is a cloth envelop collector; But the non-woven fabrics filter bag that the filtering particle diameter surpasses 5 microns particulate matter is installed detachably in the described cloth envelop collector; Described accurate filter (3) but adopt the filtering particle diameter to surpass the filter core of 1 micron particulate matter, described nf membrane strainer (4) but to adopt molecular weight cut-off be the nf membrane more than 150.
9. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 6; It is characterized in that: described preheating unit is the two-stage preheating; Plate type preheater (8) is adopted in first step preheating; Shell-and-tube preheater (9) is adopted in second stage preheating, and the condensation-water drain of the second lime set flash tank (63) is communicated with plate type preheater (8) through the lime set pump, and the non-condensable gas and the excess steam of an effect falling-film evaporator (51) and pump feed evaporator (71) are communicated with shell-and-tube preheater (9) through vacuum pump.
10. the treatment unit of highly salt containing organic waste water as claimed in claim 6 is characterized in that: described vapor recompression unit employing roots blower compressor (10) or centrifugal blower compressor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210112031.7A CN102616972B (en) | 2012-04-17 | 2012-04-17 | Comprehensive recycling method and device for high-salt-content amino acid waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210112031.7A CN102616972B (en) | 2012-04-17 | 2012-04-17 | Comprehensive recycling method and device for high-salt-content amino acid waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102616972A true CN102616972A (en) | 2012-08-01 |
| CN102616972B CN102616972B (en) | 2014-06-11 |
Family
ID=46557254
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210112031.7A Active CN102616972B (en) | 2012-04-17 | 2012-04-17 | Comprehensive recycling method and device for high-salt-content amino acid waste water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102616972B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103588338A (en) * | 2013-11-06 | 2014-02-19 | 江苏赛格尔环保工程有限公司 | High-concentration organic salt-containing wastewater treatment method adopting steam recompression technology |
| CN103626843A (en) * | 2012-08-21 | 2014-03-12 | 常州光辉生物科技有限公司 | Impurity control method for production of aspartame |
| CN103626840A (en) * | 2012-08-21 | 2014-03-12 | 常州光辉生物科技有限公司 | Preparation method for aspartame from raw materials containing chiral isomer |
| CN103642729A (en) * | 2013-12-03 | 2014-03-19 | 湖北工业大学 | Method for producing Bacillus subtilis for feeds by fermenting high-salt-content amino acid wastewater |
| CN104710033A (en) * | 2013-12-16 | 2015-06-17 | 江苏维多股份有限公司 | Aspartame production waste water processing method |
| CN104944486A (en) * | 2015-07-20 | 2015-09-30 | 周俊云 | Multifunctional sewage or waste water treatment equipment |
| CN106986358A (en) * | 2017-04-13 | 2017-07-28 | 安徽广信农化股份有限公司 | A kind of purifying technique of pyraclostrobin by-product sodium sulphate |
| CN112516822A (en) * | 2020-10-29 | 2021-03-19 | 南京工业大学 | Nanofiltration membrane and membrane performance regulation and control method based on nanocapsules |
| CN114811565A (en) * | 2022-03-22 | 2022-07-29 | 江苏润聚环保科技有限公司 | High-temperature steam condensate and flash steam dual-recycling method |
| CN116478055A (en) * | 2023-05-05 | 2023-07-25 | 新疆苏源生物工程有限公司 | Chiral refining method of aspartic acid |
| CN116946987A (en) * | 2023-09-20 | 2023-10-27 | 联仕(昆山)化学材料有限公司 | Electronic grade nitric acid preparation device and preparation process thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102050471A (en) * | 2010-11-05 | 2011-05-11 | 烟台大学 | Method for recycling sodium formate and sodium sulfite from waste sodium hydrosulfite liquid with sodium formate method |
| CN102344383A (en) * | 2011-08-18 | 2012-02-08 | 丽珠集团福州福兴医药有限公司 | Method for concentrating and crystallizing L-phenylalanine |
-
2012
- 2012-04-17 CN CN201210112031.7A patent/CN102616972B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102050471A (en) * | 2010-11-05 | 2011-05-11 | 烟台大学 | Method for recycling sodium formate and sodium sulfite from waste sodium hydrosulfite liquid with sodium formate method |
| CN102344383A (en) * | 2011-08-18 | 2012-02-08 | 丽珠集团福州福兴医药有限公司 | Method for concentrating and crystallizing L-phenylalanine |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103626843B (en) * | 2012-08-21 | 2015-10-28 | 常州光辉生物科技有限公司 | Impurity control method in a kind of aspartame production |
| CN103626843A (en) * | 2012-08-21 | 2014-03-12 | 常州光辉生物科技有限公司 | Impurity control method for production of aspartame |
| CN103626840A (en) * | 2012-08-21 | 2014-03-12 | 常州光辉生物科技有限公司 | Preparation method for aspartame from raw materials containing chiral isomer |
| CN103588338A (en) * | 2013-11-06 | 2014-02-19 | 江苏赛格尔环保工程有限公司 | High-concentration organic salt-containing wastewater treatment method adopting steam recompression technology |
| CN103642729A (en) * | 2013-12-03 | 2014-03-19 | 湖北工业大学 | Method for producing Bacillus subtilis for feeds by fermenting high-salt-content amino acid wastewater |
| CN104710033A (en) * | 2013-12-16 | 2015-06-17 | 江苏维多股份有限公司 | Aspartame production waste water processing method |
| CN104944486A (en) * | 2015-07-20 | 2015-09-30 | 周俊云 | Multifunctional sewage or waste water treatment equipment |
| CN106986358A (en) * | 2017-04-13 | 2017-07-28 | 安徽广信农化股份有限公司 | A kind of purifying technique of pyraclostrobin by-product sodium sulphate |
| CN112516822A (en) * | 2020-10-29 | 2021-03-19 | 南京工业大学 | Nanofiltration membrane and membrane performance regulation and control method based on nanocapsules |
| CN112516822B (en) * | 2020-10-29 | 2022-08-23 | 南京工业大学 | Nanofiltration membrane and membrane performance regulation and control method based on nanocapsules |
| CN114811565A (en) * | 2022-03-22 | 2022-07-29 | 江苏润聚环保科技有限公司 | High-temperature steam condensate and flash steam dual-recycling method |
| CN116478055A (en) * | 2023-05-05 | 2023-07-25 | 新疆苏源生物工程有限公司 | Chiral refining method of aspartic acid |
| CN116946987A (en) * | 2023-09-20 | 2023-10-27 | 联仕(昆山)化学材料有限公司 | Electronic grade nitric acid preparation device and preparation process thereof |
| CN116946987B (en) * | 2023-09-20 | 2024-01-12 | 联仕新材料(苏州)股份有限公司 | Electronic grade nitric acid preparation device and preparation process thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102616972B (en) | 2014-06-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102616972B (en) | Comprehensive recycling method and device for high-salt-content amino acid waste water | |
| CN102616973B (en) | Method and device for processing high-saline organic wastewater | |
| AU2007215134B2 (en) | A method for producing a distillate stream from a water stream containing at least one dissolved solid | |
| CN203428934U (en) | Concentrating and crystallizing system of copper sulfate solution | |
| CN103265089B (en) | High temperature high efficiency multi-effect seawater distillation desalination apparatus and method | |
| CN102070272A (en) | Wastewater evaporation concentration process and device system | |
| WO2009012327A2 (en) | Desalination using low-grade thermal energy | |
| CN202625969U (en) | High-salinity organic wastewater treatment device | |
| CN117185389A (en) | Concentrated crystallization desalination water treatment facilities of high salt waste water will contain through lithium bromide unit | |
| CN104399267B (en) | A kind of flash distillation wave steam recompression continuous evaporation system | |
| CN202193691U (en) | Equipment for triple-effect waste water desalination process | |
| CN202849194U (en) | Comprehensive recycling device of high-salt-content amino acid wastewater | |
| CN105439224B (en) | A kind of pressed-steam type REFRIGERATION SYSTEM DRIVEN BY CAPILLARY FORCE seawater desalination system | |
| CN104528850A (en) | Trigeneration system of fresh water, sea salt and heat energy based on deep concentration of sea water desalination strong brine | |
| CN117164037A (en) | Concentrated crystallization of high salt wastewater contains salt desalination water processing apparatus through heat pump | |
| CN112408569A (en) | Continuous treatment method of high-salinity wastewater containing sodium chloride | |
| CN204999762U (en) | Concentrated crystallization equipment of carnallite waste water | |
| CN217377356U (en) | Skid-mounted integrated evaporative crystallization system | |
| CN111661886A (en) | MVR evaporation salt separation system | |
| CN206368049U (en) | A kind of device for handling organic brine waste | |
| CN109336324B (en) | Device for preparing pure water from reverse osmosis concentrated water and working method thereof | |
| CN205974141U (en) | Desulphurization waste water treatment system | |
| CN114394706B (en) | Evaporation-freezing coupling high-concentration salt wastewater treatment method and system based on heat pump | |
| CN112870755B (en) | Potassium chloride solution concentration and crystallization production system based on waste heat of blast furnace slag flushing water and working method | |
| CN219185838U (en) | Salt lake potassium extraction MVR evaporator |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Free format text: FORMER OWNER: CHANGZHOU UNIVERSITY Effective date: 20130422 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20130422 Address after: 213127, Changzhou, Jiangsu Province town of new North waterfront industrial zone Applicant after: CHANGZHOU GUANGHUI BIOTECHNOLOGY CO.,LTD. Address before: 213127, Changzhou, Jiangsu Province town of new North waterfront industrial zone Applicant before: CHANGZHOU GUANGHUI BIOTECHNOLOGY CO.,LTD. Applicant before: Changzhou University |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170830 Address after: 213000 No. 678 ERON North Road, Xinbei District, Jiangsu, Changzhou Patentee after: CHANGZHOU GUANGHUI CHEMICAL Co.,Ltd. Address before: 213127, Changzhou, Jiangsu Province town of new North waterfront industrial zone Patentee before: CHANGZHOU GUANGHUI BIOTECHNOLOGY CO.,LTD. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200601 Address after: No.82, Anjia Zhenxing Road, Chunjiang Town, Xinbei District, Changzhou City, Jiangsu Province Patentee after: CHANGZHOU ZHONGYUAN ENGINEERING TECHNOLOGY Co.,Ltd. Address before: 213000 No. 678 ERON North Road, Xinbei District, Jiangsu, Changzhou Patentee before: CHANGZHOU GUANGHUI CHEMICAL Co.,Ltd. |
|
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 213000, No. 16 Donggang Second Road, Weicun Street, Xinbei District, Changzhou City, Jiangsu Province Patentee after: Changzhou Zhongyuan Technology Co.,Ltd. Country or region after: China Address before: 213126 No.82, Anjia Zhenxing Road, Chunjiang Town, Xinbei District, Changzhou City, Jiangsu Province Patentee before: CHANGZHOU ZHONGYUAN ENGINEERING TECHNOLOGY Co.,Ltd. Country or region before: China |