CN202849194U - Comprehensive recycling device of high-salt-content amino acid wastewater - Google Patents
Comprehensive recycling device of high-salt-content amino acid wastewater Download PDFInfo
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- CN202849194U CN202849194U CN 201220161578 CN201220161578U CN202849194U CN 202849194 U CN202849194 U CN 202849194U CN 201220161578 CN201220161578 CN 201220161578 CN 201220161578 U CN201220161578 U CN 201220161578U CN 202849194 U CN202849194 U CN 202849194U
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Abstract
The utility model provides a comprehensive recycling device of high-salt-content amino acid wastewater. The device is characterized by comprising a nano-filter separation system which is used for separating amino acid and inorganic salt, and a mechanical steam re-compression evaporation system which is used for evaporating and crystallizing inorganic salt, wherein the dense phase outlet of the nano-filter separation system is communicated with an amino acid extraction device, and the light-phase inorganic salt wastewater outlet of the nano-filter separation system is communicated with the inlet of the mechanical steam re-compression evaporation system; the oversaturated liquid outlet of the mechanical steam re-compression evaporation system is provided with a solid-liquid separation device; the liquid outlet of the solid-liquid separation device is communicated with the inlet of the nano-filter separation system; and the solid outlet of the solid-liquid separation device is communicated with a salt collection device. The comprehensive recycling device of high-salt-content amino acid wastewater is used for separating amino acid and inorganic salt by applying a nano-filter membrane, and respectively recycling the amino acid and the inorganic salt to solve the treatment problem of organic wastewater, is convenient to operate and low in treatment cost, and realizes large output with low investment.
Description
Technical field
The utility model relates to technical field of waste water processing, especially a kind of comprehensive recycling and processing device of high saliferous amino acid wastewater.
Background technology
Highly salt containing organic waste water is the difficult problem in the wastewater treatment always, extensively exists in the industries such as oil, chemical industry, food, liquid waste disposal, intermediate.Common oxygen consumption anaerobic biological is processed the restriction (general saltiness need be lower than 1%) owing to Bacterial Salt Tolerance and can't be used, and mainly takes at present multiple-effect evaporation to process.
The processing cost of multiple-effect evaporation is very high, and organism is difficult to reclaim.Polymerization at high temperature easily occurs in a lot of organism, produces foam, causes evaporation normally not carry out.Evaporating concentration process needs to 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.Vaporizer for quadruple effect, one ton of water of evaporation approximately need to consume 0.35 ton steam in the actual production, the about 15KW of power consumption, if the steam output of device is 15t/h, the market price of steam is 230 yuan/tons 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, by interchanger solution is heated to and continues heating behind the boiling point and make the solution explosive evaporatoin produce secondary steam, moisture content in the solution becomes water vapor and evaporates from solution and separate, and itself is concentrated solution.The secondary steam that evaporative process produces becomes water of condensation with cooling water condensation 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.
Function of mechanical steam recompression evaporation (Mechanical Vapor Recompression is called for short MVR) technology can be widely used in chemical industry, pharmacy, the environmental protection industry (epi), the concentrated or crystallization solution.If adopt function of mechanical steam recompression evaporation (MVR) power-saving technology, required motor power is about 660KW (pressing NaCl), energy consumption index according to Jiangsu Province, electricity price for industrial uses be 0.75 yuan/(KWh), then 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 as can be known above, adopt increasing economic efficiency that the 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 the vaporizer thermal source and substitutes bright steam.Realize the recycling of heat energy in the 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 bright steam just can make vaporizer heat energy recycling, consecutive evaporation.The MVR vaporizer also can be understood as 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 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 energy also can with the series connection of two Fans, can obtain the steam significant temp and improve about 16 ℃ so that the steam significant temp improves about 8 ℃.And the organism such as amino acid can cause the elevation of boiling point of brine waste more, thereby so that the MVR system can't move or economy reduces.The amino acid brine waste that is produced take 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 the 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 ℃ | 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 |
[0010] By above-mentioned data as can be known, amino acid can cause obvious rising to the boiling point of NaCl solution, and the higher solution boiling point that causes of amino acid concentration is higher, adopts the MVR system of two-stage fans in series when being concentrated into 40 times, will be so that effective temperature difference to only have 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 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, and is uneconomical applicable.There is no at present effective treatment process for this type of highly salt containing organic waste water.
The utility model content
The technical problems to be solved in the utility model is: a processing difficult problem that overcomes salt-containing organic wastewater in the prior art, a kind of comprehensive recycling and processing device of high saliferous amino acid wastewater is provided, after adopting nanofiltration that waste water solution is processed, 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 scheme that its technical problem that solves the utility model adopts is: 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 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 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, 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 the original fluid container by the pipeline series connection, thick level strainer, accurate filter and nano-filtration membrane filter, the concentrated phase outlet of described nano-filtration membrane filter is by the pipeline connection original fluid container, be connected with liquid supply device in the import of described original fluid container, pipeline between original fluid container and the thick level strainer is provided with concentrate pump, pipeline between accurate filter and the nano-filtration membrane filter 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 drives the drive unit of stirring rake action; Described function of mechanical steam recompression vapo(u)rization system comprises primary heater unit, an effect evaporation element, two effect evaporation element and the forced circulation evaporation unit that are communicated with by discharge pipe line successively, comprising also that the secondary steam compression that the function of mechanical steam recompression vapo(u)rization system is produced improves is input to an effect evaporation element and forced circulation evaporation unit behind the heat content again as the vapor recompression unit of thermal source, and light the 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 effect falling-film evaporator, the first vapour liquid separator and first a lime set flash tank, two effect evaporation elements comprise two effect falling-film evaporator, the second vapour liquid separator and the second lime set flash tanks, 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 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 by the lower cover of pipeline with an effect falling-film evaporator, 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 by the lower cover of pipeline with two effect falling-film evaporators, the lower cover of two effect falling-film evaporators is communicated with the upper cover of two effect falling-film evaporators 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, and the 3rd vapour liquid separator bottom is divided into two branch roads by adopting salt pump, wherein a branch road is communicated with the 3rd vapour liquid separator middle part, another branch road links to each other with the equipment for separating liquid from solid import; The condensation-water drain of one effect falling-film evaporator and pump feed evaporator is communicated with by the upper cover of pipeline with the first lime set flash tank, 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 the 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 production, the concentrated phase outlet of the nano-filtration membrane filter of described nanofiltration separation system and the pipeline between the original fluid container are provided with for temporary concentrated phase waste water and extract amino acid whose extractor, described thick level strainer is cloth envelop collector, but the non-woven fabrics filter bag that the filtering particle diameter surpasses the particulate matter of micron is installed detachably 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 nanofiltration membrane but described nano-filtration membrane filter adopts molecular weight cut-off.
For improving pre-heat effect, take full advantage of the heat energy of function of mechanical steam recompression vapo(u)rization system self, described primary heater unit is the 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 the lime set pump, and 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 by 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 beneficial effects of the utility model are, the comprehensive recycling and processing device of high saliferous amino acid wastewater of the present utility model uses nanofiltration membrane that amino acid is separated with inorganic salt, then recycle respectively, solved a processing difficult problem that contains 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 stock liquid in the vaporizer, need to provide small part to give birth to the steam during except driving, 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 to be provided, and the consumption of electric energy is far smaller than the consumption of steam energy, and power consumption reduces greatly; (2) distilled water behind the vaporizer shell side vapor condensation does not need to dispose in addition the condenser cooling, not only saved cooling circulating water, also can deliver in the preheater in addition raw material is carried out preheating, not only heat is rationally utilized, the distilled water that temperature reduces enters 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 small volume takes up an area and lacks, 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 (pressing NaCl), energy consumption index according to Jiangsu Province, electricity price for industrial uses be 0.75 yuan/(KWh), then 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 as can be known above, adopt increasing economic efficiency that the MVR system can highly significant, can help enterprise to realize target for energy-saving and emission-reduction.
Description of drawings
Below in conjunction with drawings and Examples the utility model is further specified.
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 utility model;
Fig. 2 is the functional block diagram of nanofiltration separation system among first embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present utility model;
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 utility model;
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 utility model;
Fig. 5 is the functional block diagram of nanofiltration separation system among second embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present utility model;
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 utility model;
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 utility model;
Fig. 8 is the structural representation of second embodiment of comprehensive recycling and processing device of high saliferous amino acid wastewater of the present utility model.
Among the figure: 1. original fluid container, 11. stirring rakes, 12. drive units, 13. extractor, 2. thick level strainer, 3. accurate filter, 4. nano-filtration membrane filter, 5. one imitate evaporation element, 51. an effect falling-film evaporator, 52. first vapour liquid separators, 53. first lime set flash tanks, 6. two imitate evaporation elements, 61. two effect falling-film evaporators, 62. second vapour liquid separators, 63. second lime set flash tanks, 7 forced circulation evaporation unit, 71. pump feed evaporator, 72. forced circulation pumps, 73. the 3rd vapour liquid separators, 8. plate type preheater, 9. shell-and-tube preheater.
Embodiment
By reference to the accompanying drawings the utility model is described in further detail now.These accompanying drawings are the synoptic diagram of simplification, basic structure of the present utility model only is described in a schematic way, so it only show the formation relevant with the utility model.
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 the nanofiltration separation system that separates with inorganic salt for amino acid and the function of mechanical steam 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 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, 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 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, be connected with liquid supply device in the import of 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 nano-filtration membrane filter 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 drives the drive unit 12 of stirring rake action;
The function of mechanical steam recompression vapo(u)rization system comprises primary heater unit, an effect evaporation element 5, two effect evaporation element 6 and the forced circulation evaporation unit 7 that are communicated with by discharge pipe line successively, comprising also that the secondary steam compression that the function of mechanical steam recompression vapo(u)rization system is produced improves is input to an effect evaporation element 5 and forced circulation evaporation unit 7 behind the heat content again as the vapor recompression unit of thermal source, and light the outlet mutually by discharge pipe line of nano-filtration membrane filter 4 is communicated with primary heater unit.
One effect evaporation element 5 comprises effect falling-film evaporator 51, the first vapour liquid separator 52 and first a lime set flash tank 53, two effect evaporation elements 6 comprise two effect falling-film evaporator 61, the second vapour liquid separator 62 and the second lime set flash tanks 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 by the lower cover of pipeline with an effect falling-film evaporator 51, 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 by the lower cover of pipeline with two effect falling-film evaporators 61, 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 three vapour liquid separators 73 bottoms and is divided into two branch roads by adopting salt pump, wherein a branch road is communicated with the 3rd vapour liquid separator 73 middle parts, another branch road links to each other with the 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 by the upper cover of pipeline with the first lime set flash tank 53, 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 the 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.
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 nano-filtration membrane filter 4 of nanofiltration separation system and the pipeline between the original fluid container 1 are provided with for temporary concentrated phase waste water and extract amino acid whose extractor 13.Be convenient to realize uninterrupted cyclical operation.
Thick level strainer 2 is 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 cloth envelop collector, but accurate filter 3 adopts the filter core of the particulate matter of filtering particle diameter above 1 micron, but nano-filtration membrane filter 4 employing molecular weight cut-offs are the nanofiltration membrane more than 150.
Fig. 7 is shown in Figure 8, primary heater unit is the 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, the condensation-water drain of the second lime set flash tank 63 is communicated with shell-and-tube preheater 9 by vacuum pump by 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 the roots blower compressor when loading less than 5 tons/hour, adopt the centrifugal blower compressor when loading greater than 5 tons/hour.
Set forth the present invention below in conjunction with concrete wastewater treatment: choose that to contain organic substrate concentration be 2.85%, NaCl concentration is 8.5% amino acid solution 5000L, at first carry out coarse filtration and smart 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 realized that material is concentrated, after the nanofiltration membrane filtration, can get light phase 4500L at last, its organic concentration reduces to 0.3%, and it is almost constant to contain NaCl concentration, 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 amino acid can be separated out when the suitable pH value, the solution of concentrated phase is regulated different pH values so that phenylalanine and L-Aspartic acid are separated out respectively rear utilization, when the organic concentration of last mother liquor is lower than 5%, can enter nanofiltration membrane and filter the concentrated organism of continuation, or get back to the new solution of head tank 1 adding 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 the 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 the NaCl crystal again, and the amino acid concentration in the liquid also raises, can return above-mentioned raw materials tank 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 the function of mechanical steam recompression vapo(u)rization system was concentrated to organic concentration 3%, the concentrated solution with 10% went by the nanofiltration separation system, so that organic concentration is got back to the function of mechanical steam recompression vapo(u)rization system after reducing to 0.3%.
The method that adopts nanofiltration to combine with the function of mechanical steam recompression evaporation, detect evaporating rear resulting product, shown in the detected result following table 1, test-results shows that distilled water COD part sample 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 distilled 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 as circulating cooling make-up water usefulness, realize recycling economy.
Table 1 distilled water COD (index of organic content)
Claims (6)
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 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 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, and the solid outlet of equipment for separating liquid from solid is communicated with the salinity collection device.
2. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 1, it is characterized in that: described nanofiltration separation system comprises successively the original fluid container (1) by the pipeline series connection, 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), 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 nano-filtration membrane filter (4) 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 (1), 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 primary heater unit, an effect evaporation element (5), two effect evaporation element (6) and forced circulation evaporation unit (7) that are communicated with by discharge pipe line successively, also comprises after the secondary steam compression that the function of mechanical steam recompression vapo(u)rization system is produced improves heat content being input to an effect evaporation element again
(5) and forced circulation evaporation unit (7) as the vapor recompression unit of thermal source, the light outlet mutually by discharge pipe line of described nano-filtration membrane filter (4) is communicated with primary heater unit.
3. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 2, it is characterized in that: 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), 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 by the lower cover of pipeline with an effect falling-film evaporator (51), 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 by the lower cover of pipeline with two effect falling-film evaporators (61), 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), and the 3rd vapour liquid separator (73) bottom is divided into two branch roads by adopting salt pump, wherein a branch road is communicated with the 3rd vapour liquid separator (73) middle part, another branch road links to each other with the 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 by the upper cover of pipeline with the first lime set flash tank (53), 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 the 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).
4. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 2, it is characterized in that: the concentrated phase outlet of the nano-filtration membrane filter (4) of described nanofiltration separation system and the pipeline between the original fluid container (1) are provided with for temporary concentrated phase waste water and extract amino acid whose extractor (13), described thick level strainer (2) is 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 nano-filtration membrane filter (4) but to adopt molecular weight cut-off be nanofiltration membrane more than 150.
5. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 2, it is characterized in that: described primary heater unit is the 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 the 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.
6. the comprehensive recycling and processing device of high saliferous amino acid wastewater as claimed in claim 2 is characterized in that: described vapor recompression unit employing roots blower compressor or centrifugal blower compressor.
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| CN 201220161578 CN202849194U (en) | 2012-04-17 | 2012-04-17 | Comprehensive recycling device of high-salt-content amino acid wastewater |
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| CN 201220161578 Expired - Lifetime CN202849194U (en) | 2012-04-17 | 2012-04-17 | Comprehensive recycling device of high-salt-content amino acid wastewater |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108558111A (en) * | 2018-07-03 | 2018-09-21 | 常州大学 | A kind of condensed oil sewage processing system and method |
| CN110228891A (en) * | 2019-07-22 | 2019-09-13 | 四川省川南酿造有限公司 | A kind of preparation method of brine waste MVR condensing crystallizing |
| CN115583768A (en) * | 2022-10-20 | 2023-01-10 | 江苏远方动力科技有限公司 | High-ore desalted water evaporation crystallization device and high-ore desalted water treatment method |
-
2012
- 2012-04-17 CN CN 201220161578 patent/CN202849194U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108558111A (en) * | 2018-07-03 | 2018-09-21 | 常州大学 | A kind of condensed oil sewage processing system and method |
| CN108558111B (en) * | 2018-07-03 | 2024-05-03 | 常州大学 | System and method for treating thickened oil sewage |
| CN110228891A (en) * | 2019-07-22 | 2019-09-13 | 四川省川南酿造有限公司 | A kind of preparation method of brine waste MVR condensing crystallizing |
| CN115583768A (en) * | 2022-10-20 | 2023-01-10 | 江苏远方动力科技有限公司 | High-ore desalted water evaporation crystallization device and high-ore desalted water treatment method |
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