CN102616972B - 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 PDF

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CN102616972B
CN102616972B CN201210112031.7A CN201210112031A CN102616972B CN 102616972 B CN102616972 B CN 102616972B CN 201210112031 A CN201210112031 A CN 201210112031A CN 102616972 B CN102616972 B CN 102616972B
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communicated
described
liquid separator
amino acid
pump
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CN201210112031.7A
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CN102616972A (en
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徐晨
张琳
姚洪齐
马志磊
蒋枫
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常州光辉生物科技有限公司
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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

Comprehensive recovery and treatment method and the treatment unit thereof of high saliferous amino acid wastewater

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 wastewater treatment always, in the industries such as oil, chemical industry, food, liquid waste disposal, intermediate, extensively exists.Common oxygen consumption anaerobic biological is processed restriction due to Bacterial Salt Tolerance (general saltiness need lower than 1%) and cannot be used, and mainly takes at present multiple-effect evaporation processing.

The processing cost of multiple-effect evaporation is very high, and organism is difficult to reclaim.At high temperature easily there is polymerization in a lot of organism, produces foam, causes evaporation normally not carry out.Evaporating concentration process needs to consume a large amount of raw steam always, also needs a large amount of water coolants to carry out cooling to secondary steam.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 the vaporizer of quadruple effect, in actual production, evaporate the steam that one ton of water approximately need to consume 0.35 ton, the about 15KW of power consumption, 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), within 1 year, calculate the working cost of steam approximately 9,910,000/year by 300 7200 hours working dayss.The principle of work of conventional vaporizer is to make thermal source with the fresh steam of boiler for producing, after solution being heated to boiling point by interchanger, continuation heating makes solution explosive evaporatoin produce secondary steam, moisture content in solution becomes water vapor and evaporates and separate from solution, and itself is concentrated solution.The secondary steam that evaporative process produces becomes water of condensation by cooling water condensation again, and the thermal energy transfer in secondary steam causes thermal waste and cooling-water consumption to being diffused in water coolant again in air.

Function of mechanical steam recompression evaporation (Mechanical Vapor Recompression is called for short MVR) technology, can be widely used in chemical industry, pharmacy, environmental protection industry (epi), concentrated solution or crystallization.If adopt function of mechanical steam recompression evaporation (MVR) power-saving technology, required motor power is about 660KW (by NaCl), according to the energy consumption index of Jiangsu Province, electricity price for industrial uses be 0.75 yuan/(KWh), the annual required working cost of MVR system is 3,560,000/year, and the running cost of relatively common multiple-effect saving is about for 6,350,000/year.By more known above, adopt increasing economic efficiency that MVR system can highly significant, realize target for energy-saving and emission-reduction.The principle of work of function of mechanical steam recompression evaporation (MVR) vaporizer is to utilize compressor that the secondary steam of vaporizer generation is compressed its pressure and temperature is raise, and then makes vaporizer thermal source and substitutes fresh steam.Realize the recycling of heat energy in secondary steam, make the heat energy recycling of vaporizer.As long as a small amount of power driven compressor work is provided, do not need fresh steam just can make vaporizer heat energy recycling, consecutive evaporation.In thermodynamics, MVR vaporizer also can be understood as open type heat pump.The effect of compressor is not to produce the heat that evaporation needs, but upgrades and carry the heat of vaporizer to form heat circulation.MVR vaporizer is vaporizer technology of new generation, is a kind of new and high technology of energy-conserving and environment-protective.

In MVR system, the centrifugal fans that adopt improve steam enthalpy more at present, and general separate unit can make steam significant temp improve 8 DEG C of left and right, also can, with two Fans series connection, can obtain steam significant temp and improve 16 DEG C of left and right.And the organism such as amino acid can cause the elevation of boiling point of brine waste more, thereby MVR system cannot be moved or economy reduction.The amino acid brine waste being produced taking production aspartame device is as example, and amino acid brine waste composition is as follows: 0.1%~0.2% phenylalanine; 0.1~0.2%L-aspartic acid; Sodium-chlor 8~9%; PH=6.8-7.5.Waste water has been done to boiling point test, and data are as follows:

NaCl concentration % ??8.5 ??10 ??11.9 ??15.1 ??20.97 ??24.8 ??28.92 Atmospheric boiling point DEG C ??101.5 ??102.2 ??102.8 ??103.7 ??105.8 ??108 ??110.2

When cycles of concentration is 30 times, boiling point is 111.8 degree, and when cycles of concentration is 40 times, boiling point is 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 DEG C ??101 ??102 ??103 ??104 ??105 ??107 ??108

From above-mentioned data, amino acid can cause obvious rising to the boiling point of NaCl solution, and the higher solution boiling point causing of amino acid concentration is higher, adopts the MVR system of two-stage fans in series in the time being concentrated into 40 times, will make effective temperature difference only have 1 DEG C, heat exchange cannot be carried out.Now MVR technology can not be used further to the processing of the waste water that this type organic solubility is higher, can only be used at most the evaporation concentration of waste water.If adopt the MVR system of force 3 wind machine series connection, although heat exchange is feasible, energy consumption improves greatly, and equipment investment is larger, uneconomical being suitable for.There is no at present effective treatment process for this type of highly salt containing organic waste water.

Summary of the invention

The technical problem to be solved in the present invention is: a processing difficult problem that overcomes salt-containing organic wastewater in 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 to process waste water solution, organism is separated with inorganic salt, reduce organism to the ebullioscopic impact of waste water, be conducive to the evaporation process of brine waste.

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 aspartame industry salt-containing organic wastewater by strainer exceedes the granule foreign of 1 micron;

2. separation of organic substances and inorganics: adopt 8 inches of nanofiltration membrane, single membrane flux is at 8~12 cubes ms/h, pressure 2~4MPa, 20~50 DEG C of temperature, filter the aspartame industry salt-containing organic wastewater of having removed granule foreign, collect respectively concentrated phase waste water and light phase waste water;

3. reclaim organism and extract salinity: the concentrated phase waste water by step in 2. carries out iso-electric point adjusting, and pH value is adjusted at 5.0~6.0 o'clock and separates out phenylalanine, and takes out phenylalanine, separates out L-Aspartic acid, and take out L-Aspartic acid when pH value is adjusted to 2.7-2.9; Light phase waste water by step in 2. adopts function of mechanical steam recompression vapo(u)rization system to carry out evaporation concentration and obtains supersaturated solution, in supersaturated solution, isolate NaCl, function of mechanical steam recompression vapo(u)rization system does not need the external world that thermal source is provided after starting, the secondary steam that system self produces is recompressed and is improved heat content by machinery as thermal source, ensures raw material evaporation concentration in system;

4. circular treatment: isolate amino acid whose concentrated phase waste water in step in 3. and isolate in the waste water of salinity and fill into the new high saliferous amino acid wastewater of aspartame industry again by above-mentioned steps cyclical operation.

Step is talked phase waste water described in 3. carrying out first carrying out preheating before the evaporation of function of mechanical steam recompression vapo(u)rization system.

Adopt the water of condensation of function of mechanical steam recompression vapo(u)rization system self to carry out preliminary preheating to light phase waste water, adopt non-condensable gas and the excess steam of function of mechanical steam recompression vapo(u)rization system self to carry out preheating again to light phase waste water, after the preheating of light phase waste water, temperature is 81~82 DEG C.

Described function of mechanical steam recompression vapo(u)rization system adopts negative-pressure operation.

A kind of comprehensive recycling and processing device of high saliferous amino acid wastewater, comprise the nanofiltration separation system that separates with inorganic salt for amino acid and the function of mechanical steam recompression vapo(u)rization system for inorganic salt evaporative crystallization, the concentrated phase outlet of described nanofiltration separation system is communicated with amino acid extraction element, the light phase inorganic salt wastewater outlet of described nanofiltration separation system is communicated with the import of function of mechanical steam recompression vapo(u)rization system, the supersaturated solution outlet of described function of mechanical steam 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, the solid outlet of equipment for separating liquid from solid is communicated with salinity collection device.

Concrete, described nanofiltration separation system comprises the original fluid container of connecting by pipeline successively, thick level strainer, accurate filter and nano-filtration membrane filter, the concentrated phase outlet of described nano-filtration membrane filter is by pipeline connection original fluid container, in the import of described original fluid container, be connected with liquid supply device, pipeline between original fluid container and thick level strainer is provided with concentrate pump, pipeline between accurate filter and nano-filtration membrane filter is provided with topping-up pump, in the tank body of described original fluid container, be provided with the whipping appts that waste water is mixed, described whipping appts comprises stirring rake and drives the drive unit of stirring rake action, described function of mechanical steam recompression vapo(u)rization system comprises the primary heater unit by discharge pipe line UNICOM, an effect evaporation element, two effect evaporation element and forced circulation evaporation unit successively, also comprise and will after the secondary steam compression raising heat content of function of mechanical steam recompression vapo(u)rization system generation, be input to an effect evaporation element and the forced circulation evaporation unit vapor recompression unit as thermal source again, the light outlet mutually by discharge pipe line of described nano-filtration membrane filter is communicated with primary heater unit.

Further, a described effect evaporation element comprises an effect falling-film evaporator, the first vapour liquid separator and the first lime set flash tank, two effect evaporation elements comprise two effect falling-film evaporators, the second vapour liquid separator and the second lime set flash tank, and 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 the first vapour liquid separator and the second vapour liquid separator respectively by pipeline, the bottom concentrated solution outlet of the first vapour liquid separator is communicated with the lower cover of an effect falling-film evaporator by pipeline, the vapour outlet of the first vapour liquid separator is communicated with the upper cover of two effect falling-film evaporators, the second vapour liquid separator bottom concentrated solution outlet is communicated with the lower cover of two effect falling-film evaporators by pipeline, the lower cover of two effect falling-film evaporators is communicated with the two effect upper covers of falling-film evaporator and the upper cover of pump feed evaporator through the second recycle pump, the upper cover of pump feed evaporator is communicated with the 3rd vapour liquid separator by pipeline, the lower cover of pump feed evaporator connects forced circulation pump, the 3rd vapour liquid separator bottom is divided into two articles of branch roads by adopting salt pump, wherein one article of branch road is communicated with the 3rd vapour liquid separator middle part, another branch road is connected with equipment for separating liquid from solid import, 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 by pipeline, the vapour outlet of the first lime set flash tank is communicated with the upper cover of two effect falling-film evaporators, and the condensation-water drain of the first lime set flash tank and two effect falling-film evaporators is communicated with the upper cover of the second lime set flash tank, the vapour outlet of the second vapour liquid separator, the 3rd vapour liquid separator and the second lime set flash tank is communicated with vapor recompression unit, and the vapour outlet of vapor recompression unit is communicated with the steam inlet of an effect falling-film evaporator and pump feed evaporator.

Further improve filter effect, and realize uninterrupted serialization and produce, pipeline between concentrated phase outlet and the original fluid container of the nano-filtration membrane filter of described nanofiltration separation system is provided with for temporary concentrated phase waste water and extracts amino acid whose extractor, described thick level strainer is cloth envelop collector, the non-woven fabrics filter bag of the particulate matter that can filtering particle diameter exceedes micron is detachably installed in described cloth envelop collector, described accurate filter adopts the filter core that can filtering particle diameter exceedes the particulate matter of micron, it can molecular weight cut-off be above nanofiltration membrane that described nano-filtration membrane filter adopts.

For improving pre-heat effect, make full use of the heat energy of function of mechanical steam recompression vapo(u)rization system self, described primary heater unit is two-stage preheating, the pre-thermal recovery plate type preheater of the first step, the second stage pre-thermal recovery shell-and-tube preheater, the condensation-water drain of the second lime set flash tank is communicated with plate type preheater by lime set pump, and non-condensable gas and the excess steam of an effect falling-film evaporator and pump feed evaporator are communicated with shell-and-tube preheater by vacuum pump.

As preferably, described vapor recompression unit adopts roots blower compressor in the time that load is less than 5 tons of/hour; Load adopts centrifugal blower compressor while being greater than 5 tons of/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 thereof use nanofiltration membrane that amino acid is separated with inorganic salt, then recycle respectively, solve the processing difficult problem containing organic waste water, easy to operate, processing cost is low, and small investment realizes larger output.

Advantage is: (1) is from separator secondary steam out, improve heat content through compressor, temperature raises, and is re-used as the heat source of vaporizer, carries out heat exchange with the stock liquid in vaporizer, during except driving, need to provide the raw steam of small part, system needed thermal source in service is all settled a dispute by the parties concerned themselves by system, does not need to supplement in addition raw steam, and the electric energy of compressor operating only need to be provided, and the consumption of electric energy is far smaller than the consumption of steam energy, power consumption reduces greatly; (2) not need to configure in addition condenser cooling for the distilled water after vaporizer shell side vapor condensation, not only save cooling circulating water, also can deliver in preheater raw material is carried out to preheating in addition, not only heat is rationally utilized, the distilled water that temperature reduces enters industrial cycle pond, and as other process water, water resources also obtains reasonable recycle, system operation running cost reduces greatly, energy saving economy remarkable benefit; (3) whole evaporation separation system small volume, takes up an area less, and technical process is simple, efficient, energy-conservation.

Adopt function of mechanical steam recompression evaporation (MVR) power-saving technology, required motor power is about 660KW (by NaCl), according to the energy consumption index of Jiangsu Province, electricity price for industrial uses be 0.75 yuan/(KWh), the annual required working cost of MVR system is 3,560,000/year, and the running cost of relatively common multiple-effect saving is about for 6,350,000/year.By more known above, adopt increasing economic efficiency that MVR system can highly significant, can help enterprise to realize target for energy-saving and emission-reduction.

Brief description of the drawings

Below in conjunction with drawings and Examples, the present invention is further described.

Fig. 1 is the functional 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 functional block diagram of nanofiltration separation system in 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 in first embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;

Fig. 4 is the functional 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 functional block diagram of nanofiltration separation system in 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 in second embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention;

Fig. 7 is the functional block diagram of function of mechanical steam 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.

In figure: 1. original fluid container, 11. stirring rakes, 12. drive units, 13. extractors, 2. thick grade of strainer, 3. accurate filter, 4. nano-filtration membrane filter, 5. an effect evaporation element, 51. 1 effect falling-film evaporators, 52. first vapour liquid separators, 53. first lime set flash tanks, 6. two effect evaporation elements, 61. 2 effect falling-film evaporators, 62. second vapour liquid separators, 63. second lime set flash tanks, 7 forced circulation evaporation unit, 71. pump feed evaporators, 72. forced circulation pumps, 73. the 3rd vapour liquid separators, 8. plate type preheater, 9. shell-and-tube preheater, 10. roots blower compressor.

In Fig. 7 Fig. 8: waste water---

Water of condensation--------

Steam-------

Embodiment

In conjunction with the accompanying drawings, the present invention is further detailed explanation.These accompanying drawings are the schematic diagram of simplification, and basic structure of the present invention is only described in a schematic way, and therefore it only shows 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 aspartame industry salt-containing organic wastewater by strainer exceedes the granule foreign of 1 micron;

2. separation of organic substances and inorganics: adopt 8 inches of nanofiltration membrane, single membrane flux is at 8~12 cubes ms/h, pressure 2~4MPa, 20~50 DEG C of temperature, filter the aspartame industry salt-containing organic wastewater of having removed granule foreign, collect respectively concentrated phase waste water and light phase waste water;

3. reclaim organism and extract salinity: the concentrated phase waste water by step in 2. carries out iso-electric point adjusting, and pH value is adjusted at 5.0~6.0 o'clock and separates out phenylalanine, and takes out phenylalanine, separates out L-Aspartic acid, and take out L-Aspartic acid when pH value is adjusted to 2.7-2.9; Light phase waste water by step in 2. adopts function of mechanical steam recompression vapo(u)rization system to carry out evaporation concentration and obtains supersaturated solution, isolates NaCl in supersaturated solution;

4. circular treatment: isolate amino acid whose concentrated phase waste water in step in 3. and isolate in the waste water of salinity and fill into the new high saliferous amino acid wastewater of aspartame industry again by above-mentioned steps cyclical operation.

Further, step is talked phase waste water described in 3. carrying out first carrying out preheating before the evaporation of function of mechanical steam recompression vapo(u)rization system.Adopt the water of condensation of function of mechanical steam recompression vapo(u)rization system self to carry out preliminary preheating to light phase waste water, adopt non-condensable gas and the excess steam of function of mechanical steam recompression vapo(u)rization system self to carry out preheating again to light phase waste water, after the preheating of light phase waste water, temperature is 81~82 DEG C.

For reducing energy consumption, described function of mechanical steam recompression vapo(u)rization system adopts negative-pressure operation.

First embodiment of the comprehensive recycling and processing device of high saliferous amino acid wastewater of the present invention shown in Fig. 1 Fig. 2 Fig. 3, comprise the nanofiltration separation system that separates with inorganic salt for amino acid and the function of mechanical steam recompression vapo(u)rization system for inorganic salt evaporative crystallization, the concentrated phase outlet of nanofiltration separation system is communicated with amino acid extraction element, the light phase inorganic salt wastewater outlet of nanofiltration separation system is communicated with the import of function of mechanical steam recompression vapo(u)rization system, the supersaturated solution outlet of function of mechanical steam 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, the solid outlet of equipment for separating liquid from solid is communicated with salinity collection device.

Shown in Fig. 2, nanofiltration separation system comprises the original fluid container 1 of connecting by pipeline successively, thick level strainer 2, accurate filter 3 and nano-filtration membrane filter 4, the concentrated phase outlet of nano-filtration membrane filter 4 is by pipeline connection original fluid container 1, in the import of original fluid container 1, be connected with liquid supply device, pipeline between original fluid container 1 and thick level strainer 2 is provided with concentrate pump, pipeline between accurate filter 3 and nano-filtration membrane filter 4 is provided with topping-up pump, in the tank body of original fluid container 1, be provided with the whipping appts that waste water is mixed, whipping appts comprises stirring rake 11 and drives the drive unit 12 of stirring rake action,

Function of mechanical steam recompression vapo(u)rization system comprises the primary heater unit by discharge pipe line UNICOM, an effect evaporation element 5, two effect evaporation element 6 and forced circulation evaporation unit 7 successively, also comprise and will after the secondary steam compression raising heat content of function of mechanical steam recompression vapo(u)rization system generation, be input to an effect evaporation element 5 and the forced circulation evaporation unit 7 vapor recompression unit as thermal source again, the light outlet mutually by discharge pipe line of nano-filtration membrane filter 4 is communicated with primary heater unit.

One effect evaporation element 5 comprises an effect falling-film evaporator 51, the first vapour liquid separator 52 and the first lime set flash tank 53, two effect evaporation elements 6 comprise two effect falling-film evaporators 61, the 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 the first vapour liquid separator 52 and the second vapour liquid separator 62 respectively by pipeline, the bottom concentrated solution outlet of the first vapour liquid separator 52 is communicated with the lower cover of an effect falling-film evaporator 51 by pipeline, the vapour outlet of the first vapour liquid separator 52 is communicated with the upper cover of two effect falling-film evaporators 61, the second vapour liquid separator 62 bottom concentrated solution outlets are communicated with the lower cover of two effect falling-film evaporators 61 by pipeline, the lower cover of two effect falling-film evaporators 61 is communicated with the two effect upper covers of falling-film evaporator 61 and the upper cover of pump feed evaporator 71 through the second recycle pump, the upper cover of pump feed evaporator 71 is communicated with the 3rd vapour liquid separator 73 by pipeline, the lower cover of pump feed evaporator 71 connects forced circulation pump 72, the 3rd vapour liquid separator 73 bottoms are divided into two articles of branch roads by adopting salt pump, wherein one article of branch road is communicated with the 3rd vapour liquid separator 73 middle parts, another branch road is connected with equipment for separating liquid from solid import, 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 by pipeline, the vapour outlet of the first lime set flash tank 53 is communicated with the upper cover of two effect falling-film evaporators 61, and the condensation-water drain of the first lime set flash tank 53 and two effect falling-film evaporators 61 is communicated with the upper cover of the second lime set flash tank 63, the vapour outlet of the second vapour liquid separator 62, the 3rd vapour liquid separator 73 and the second lime set flash tank 63 is communicated with vapor recompression unit, and the vapour outlet of vapor recompression unit is communicated with the steam inlet of an effect falling-film evaporator 51 and pump feed evaporator 71.

Shown in Fig. 4 Fig. 5 Fig. 6, be second embodiment of the present invention, and the difference of first embodiment is: the pipeline between concentrated phase outlet and the original fluid container 1 of the nano-filtration membrane filter 4 of nanofiltration separation system is provided with for temporary concentrated phase waste water and extracts amino acid whose extractor 13.Be convenient to realize uninterrupted cyclical operation.

Thick level strainer 2 is cloth envelop collector, the non-woven fabrics filter bag that can filtering particle diameter exceedes the particulate matter of 5 microns is detachably installed in cloth envelop collector, accurate filter 3 adopts the filter core that can filtering particle diameter exceedes the particulate matter of 1 micron, and it can molecular weight cut-off be more than 150 nanofiltration membrane that nano-filtration membrane filter 4 adopts.

Shown in Fig. 7 Fig. 8, primary heater unit is two-stage preheating, the pre-thermal recovery plate type preheater 8 of the first step, the second stage pre-thermal recovery shell-and-tube preheater 9, non-condensable gas and excess steam that the condensation-water drain of the second lime set flash tank 63 is communicated with plate type preheater 8, one effect falling-film evaporators 51 and pump feed evaporator 71 by lime set pump are communicated with shell-and-tube preheater 9 by vacuum pump.

Vapor recompression unit adopts roots blower compressor 10 in the time that load is less than 5 tons of/hour, adopts centrifugal blower compressor in the time that load is greater than 5 tons of/hour.

Set forth the present invention below in conjunction with concrete wastewater treatment: choosing containing organic concentration is 2.85%, NaCl concentration is 8.5% amino acid solution 5000L, first carry out coarse filtration and essence filter, remove particulate matter, then adopt nanofiltration membrane to filter, NaCl and water molecule energy see through nanofiltration membrane and obtain light phase, amino acid is because molecule is trapped within more greatly concentrated phase, thereby it is concentrated to have realized material, after nanofiltration membrane is filtered, finally can obtain light phase 4500L, its organic concentration reduces to 0.3%, and it is almost constant containing NaCl concentration, now the solution of light phase also directly carries out evaporative crystallization and obtains salinity, and concentrated phase organic concentration becomes 25.8%.Because amino acid can be separated out when the suitable pH value, regulate different pH values to make phenylalanine and L-Aspartic acid separate out respectively rear utilization the solution of concentrated phase, the organic concentration of last mother liquor is lower than 5% time, can enter nanofiltration membrane and filter the concentrated organism of continuation, or get back to head tank 1 and add new solution again by above-mentioned steps, realize uninterrupted circular treatment.The solution of other different concns can adopt aforesaid method to carry out separating of amino acid and inorganic salt, does not repeat them here.

The solution of light phase adopts function of mechanical steam recompression vapo(u)rization system to carry out evaporative crystallization, concentrated step by step, until form the supersaturated solution of NaCl, carry out solid-liquid separation, solid is NaCl crystal again, and the amino acid concentration in liquid also raises, can return above-mentioned raw materials tank 1 circulates, for making vapo(u)rization system heat exchange feasible, generally need to control organic content in 3%, it is in 9 degree that experiment obtains the elevation of boiling point.In the time that function of mechanical steam recompression vapo(u)rization system is concentrated to organic concentration 3%, 10% concentrated solution is gone by nanofiltration separation system, get back to function of mechanical steam recompression vapo(u)rization system after making organic concentration reduce to 0.3%.

Adopt nanofiltration to evaporate with function of mechanical steam recompression the method combining, the product obtaining after evaporating is detected, shown in detected result following table 1, test-results shows that distilled water COD part sample numerical value is higher, because liquid level in experiment is too high or seethed with excitement and acutely cause, in actual production, can avoid, bigger device can make distilled water COD maintain below 500, and this water adds sterilization and just can reach the water quality requirement of cooling circulating water with common biochemical treatment, thereby as circulating cooling make-up water use, realize recycling economy.

Table 1 distilled water COD (index of organic content)

Taking above-mentioned foundation desirable embodiment of the present invention as enlightenment, by above-mentioned description, relevant staff can, not departing from the scope of this invention technological thought, carry out various change and amendment completely.The technical scope of this invention is not limited to the content on specification sheets, must determine its technical scope according to claim scope.

Claims (3)

1. the comprehensive recycling and processing device of a high saliferous amino acid wastewater, it is characterized in that: comprise the nanofiltration separation system that separates with inorganic salt for amino acid and the function of mechanical steam recompression vapo(u)rization system for inorganic salt evaporative crystallization, the concentrated phase outlet of described nanofiltration separation system is communicated with amino acid extraction element, the light phase inorganic salt wastewater outlet of described nanofiltration separation system is communicated with the import of function of mechanical steam recompression vapo(u)rization system, the supersaturated solution outlet of described function of mechanical steam 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, the solid outlet of equipment for separating liquid from solid is communicated with salinity collection device,
Described nanofiltration separation system comprises the original fluid container (1) of connecting by pipeline successively, thick level strainer (2), accurate filter (3) and nano-filtration membrane filter (4), the concentrated phase outlet of described nano-filtration membrane filter (4) is by pipeline connection original fluid container (1), in the import of described original fluid container (1), be connected with liquid supply device, pipeline between original fluid container (1) and thick level strainer (2) is provided with concentrate pump, pipeline between accurate filter (3) and nano-filtration membrane filter (4) is provided with topping-up pump, in the tank body of described original fluid container (1), be provided with the whipping appts that waste water is mixed, described whipping appts comprises stirring rake (11) and drives the drive unit (12) of stirring rake (11) action,
Described function of mechanical steam recompression vapo(u)rization system comprises the primary heater unit by discharge pipe line UNICOM, an effect evaporation element (5), two effect evaporation elements (6) and forced circulation evaporation unit (7) successively, also comprise and will after the secondary steam compression raising heat content of function of mechanical steam recompression vapo(u)rization system generation, be input to an effect evaporation element (5) and forced circulation evaporation unit (7) the vapor recompression unit as thermal source again, the light outlet mutually by discharge pipe line of described nano-filtration membrane filter (4) is communicated with primary heater unit;
A described effect evaporation element (5) comprises an effect falling-film evaporator (51), the first vapour liquid separator (52) and the first lime set flash tank (53), two effect evaporation elements (6) comprise two effect falling-film evaporators (61), the 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 the first vapour liquid separator (52) and the second vapour liquid separator (62) respectively by pipeline, the bottom concentrated solution outlet of the first vapour liquid separator (52) is communicated with the lower cover of an effect falling-film evaporator (51) by pipeline, the vapour outlet of the first vapour liquid separator (52) is communicated with the upper cover of two effect falling-film evaporators (61), the second vapour liquid separator (62) bottom concentrated solution outlet is communicated with the lower cover of two effect falling-film evaporators (61) by pipeline, the lower cover of two effect falling-film evaporators (61) is communicated with the upper cover of two effect falling-film evaporators (61) and the upper cover of pump feed evaporator (71) through the second recycle pump, the upper cover of pump feed evaporator (71) is communicated with the 3rd vapour liquid separator (73) by pipeline, the lower cover of pump feed evaporator (71) connects forced circulation pump (72), the 3rd vapour liquid separator (73) bottom is divided into two articles of branch roads by adopting salt pump, wherein one article of branch road is communicated with the 3rd vapour liquid separator (73) middle part, another branch road is connected with equipment for separating liquid from solid import,
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) by pipeline, the vapour outlet of the first lime set flash tank (53) is communicated with the upper cover of two effect falling-film evaporators (61), and the condensation-water drain of the first lime set flash tank (53) and two effect falling-film evaporators (61) is communicated with the upper cover of the second lime set flash tank (63);
The vapour outlet of the second vapour liquid separator (62), the 3rd vapour liquid separator (73) and the second lime set flash tank (63) is communicated with vapor recompression unit, and the vapour outlet of vapor recompression unit is communicated with the steam inlet of an effect falling-film evaporator (51) and pump feed evaporator (71);
Pipeline between concentrated phase outlet and the original fluid container (1) of the nano-filtration membrane filter (4) of described nanofiltration separation system is provided with for temporary concentrated phase waste water and extracts amino acid whose extractor (13), described thick level strainer (2) is cloth envelop collector, the non-woven fabrics filter bag that can filtering particle diameter exceedes the particulate matter of 5 microns is detachably installed in described cloth envelop collector, described accurate filter (3) adopts the filter core that can filtering particle diameter exceedes the particulate matter of 1 micron, it can molecular weight cut-off be more than 150 nanofiltration membrane that described nano-filtration membrane filter (4) adopts.
2. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 1, it is characterized in that: described primary heater unit is two-stage preheating, the pre-thermal recovery plate type preheater of the first step (8), the second stage pre-thermal recovery shell-and-tube preheater (9), the condensation-water drain of the second lime set flash tank (63) is communicated with plate type preheater (8) by lime set pump, and 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) by vacuum pump.
3. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 1, is characterized in that: described vapor recompression unit adopts roots blower compressor (10) or centrifugal blower compressor.
CN201210112031.7A 2012-04-17 2012-04-17 Comprehensive recycling method and device for high-salt-content amino acid waste water CN102616972B (en)

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