CN217103446U - High salt waste water evaporation crystallization of coal industry divides salt device - Google Patents
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Abstract
The utility model relates to a coal chemical industry water treatment technical field, concretely relates to high salt waste water evaporation crystallization of coal chemical industry divides salt device. The raw material liquid passes through a first feeding pump, a first heater, a first circulating pump, a first-stage separator, a sodium sulfate thickener, a sodium sulfate centrifuge and is centrifuged to obtain sodium sulfate, the liquid of the sodium sulfate centrifuge reaches a sodium sulfate mother liquid tank and then enters a single-effect feeding pump, a second-stage flash separator, a sodium chloride thickener and a sodium chloride centrifuge to be centrifuged to obtain sodium chloride. And centrifuging the nanofiltration clear liquid by a second feeding pump, a forced heater, a second circulating pump, a forced separator, a single-effect evaporation separator, a sodium chloride thickener and a sodium chloride centrifuge to obtain sodium chloride. And the liquid of the sodium chloride centrifuge reaches a sodium chloride mother liquor tank, then enters a cooling thickener through a sodium chloride mother liquor pump, and then enters a sodium nitrate centrifuge to centrifuge out sodium nitrate. The utility model discloses beneficial effect does: the system can better control the concentration and the proportion of each component in the evaporation process.
Description
Technical Field
The utility model relates to a coal chemical industry water treatment technical field, concretely relates to high salt waste water evaporation crystallization of coal chemical industry divides salt device.
Background
The coal chemical industry has the biggest characteristics of huge waste water amount, complex waste water quality, high pollutant concentration and large treatment difficulty. The wastewater of coal chemical industry after deaminizing nitrogen and COD is collectively called as the wastewater of high strong salt of coal chemical industry with the sewage discharged by circulating sewage and chemical water station. At present, the treatment of the high-salinity wastewater in the coal chemical industry is realized by the distributed crystallization, and the treatment and the recycling are realized by firstly purifying and then carrying out the distributed crystallization.
The common method for coal chemical wastewater treatment projects in the market at present is to separate divalent salt by nanofiltration, separate sodium chloride and sodium sulfate and then evaporate and crystallize. However, in this treatment process, the purification effect is insufficient, and when crystallization is performed, substances affecting crystallization are present in the wastewater, which results in a decrease in the amount of crystallization, a decrease in efficiency, failure to meet actual crystallization requirements, and an unexpected actual effect.
Therefore, the salt separation crystallization treatment device for the high-salinity wastewater in the coal chemical industry is proposed to solve the problems.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to prior art's defect and not enough, provide a high salt waste water evaporative crystallization of coal industry divides salt device, this system adopts high temperature evaporative concentration crystallization and freezing crystallization technology, and in the feed liquid evaporative concentration process, the adoption is strained, is evaporated, three kinds of modes of freezing carry out the combined treatment, adopts forced circulation evaporation form, high-efficient refrigerant cooling arrangement, high-efficient separation crystallization method. Three components of sodium nitrate, sodium chloride and sodium sulfate contained in the wastewater are recovered. The system can better control the concentration and the proportion of each component in the evaporation process, so that the concentration and the proportion deviate from a common saturation curve to carry out evaporation crystallization, and the purity of the crystallized salt is greatly improved.
In order to achieve the above purpose, the utility model adopts the following technical scheme: a device for separating salt from high-salinity wastewater in coal chemical industry through evaporative crystallization comprises a first feeding pump 101, wherein the output end of the first feeding pump 101 is connected with a first heater 102 through a pipeline, the output end of the first heater 102 is connected with a first circulating pump 103 through a pipeline, the output end of the first circulating pump 103 is connected with a first-stage separator 105 through a pipeline, the output end of the first-stage separator 105 is connected with a sodium sulfate thickener 106 through a pipeline, the output end of the sodium sulfate thickener 106 is connected with a sodium sulfate centrifuge 107 through a pipeline, the output end of the sodium sulfate centrifuge 107 is connected with a sodium sulfate mother liquor tank 108 through a pipeline, the output end of the sodium sulfate mother liquor tank 108 is connected with a single-effect feeding pump 109 through a pipeline, the output end of the single-effect feeding pump 109 is connected with a second-stage flash separator 110 through a pipeline, and the output end of the second-stage flash separator 110 is connected with a first sodium chloride thickener 111 through a pipeline, the output end of the first sodium chloride thickener 111 is connected with a first sodium chloride centrifuge 112 through a pipeline, the output end of the first sodium chloride centrifuge 112 is connected with a first sodium chloride mother liquor tank 113 through a pipeline, the output end of the first sodium chloride mother liquor tank 113 is connected with a second feeding pump 201 through a pipeline, the output end of the second feeding pump 201 is connected with a forced heater 202 through a pipeline, the output end of the forced heater 202 is connected with a second circulating pump 203 through a pipeline, the output end of the second circulating pump 203 is connected with a forced separator 205 through a pipeline, the output end of the forced separator 205 is connected with a single-effect evaporation separator 206 through a pipeline, the output end of the single-effect evaporation separator 206 is connected with a second sodium chloride thickener 207 through a pipeline, the output end of the second sodium chloride thickener 207 is connected with a second sodium chloride centrifuge 208 through a pipeline, the output end of the second sodium chloride centrifuge 208 is connected with a second sodium chloride mother liquor tank 209 through a pipeline, the output of second sodium chloride mother liquor jar 209 has sodium chloride mother liquor pump 211 through the pipe connection, the output of sodium chloride mother liquor pump 211 has cooling stiff ware 212 through the pipe connection, the output of cooling stiff ware 212 has sodium nitrate centrifuge 213 through the pipe connection, sodium nitrate centrifuge 213's output has sodium nitrate mother liquor jar 214 through the pipe connection, the output of sodium nitrate mother liquor jar 214 has sodium nitrate mother liquor jar 215 through the pipe connection, the output of sodium nitrate mother liquor jar 215 passes through the pipeline and is connected with the material input of single-effect evaporation separator 206.
The first-stage separator 105 is provided with a first-stage separator gas-phase outlet 1051 and a first-stage separator liquid-phase outlet 1052, and the first-stage separator liquid-phase outlet 1052 is connected with the input end of the sodium sulfate thickener 106 through a pipeline.
The gas phase outlet 1051 of the first-stage separator is connected with a first compressor 104 through a pipeline, and the output end of the first compressor 104 is connected with the steam input end of the first heater 102 through a pipeline.
The sodium sulfate centrifuge 107 is provided with a sodium sulfate crystal outlet 1071 and a sodium sulfate liquid phase outlet 1072, and the sodium sulfate liquid phase outlet 1072 is connected with the input end of a sodium sulfate mother liquor tank 108 through a pipeline.
The secondary flash evaporation separator 110 is provided with a flash evaporator gas phase outlet 1101, the flash evaporator gas phase outlet 1101 is connected with the first intercooler 114 through a pipeline, and the secondary steam after flash evaporation is fully cooled through the first intercooler 114.
The forced separator 205 is provided with a forced separator gas phase outlet 2051 and a forced separator liquid phase outlet 2052, and the forced separator liquid phase outlet 2052 is connected with the input end of the single-effect evaporation separator 206 through a pipeline.
The gas phase outlet 2051 of the forced separator is connected with a second compressor 204 through a pipeline, and the output end of the second compressor 204 is connected with the steam input end of the second heater 202 through a pipeline.
The single-effect evaporation separator 206 is provided with an evaporator gas-phase outlet 2061, the evaporator gas-phase outlet 2061 is connected with the second intercooler 210 through a pipeline, and the evaporated secondary steam is fully cooled by the second intercooler 210.
The sodium nitrate centrifuge 213 is provided with a sodium nitrate crystal outlet 2131 and a sodium nitrate liquid phase outlet 2132, and the sodium nitrate liquid phase outlet 2132 is connected with the input end of a sodium nitrate mother liquor tank 214 through a pipeline.
The utility model discloses a theory of operation: the flow direction of the nanofiltration concentrated solution evaporation crystallization salt separation material is as follows: the raw material liquid enters a first heater 102 for heating after passing through a first feeding pump 101, and then enters a first-stage separator 105 after passing through a first circulating pump 103, and secondary steam is pressurized by a compressor 4 and then returns to the first heater 102 again for heating. After the heated material is evaporated and concentrated in the first-stage separator 105, the material containing crystals enters a sodium sulfate thickener 106 and then enters a sodium sulfate centrifuge 107 to centrifuge out sodium sulfate, the liquid in the sodium sulfate centrifuge 107 reaches a sodium sulfate mother liquor tank 108 and then enters a single-effect feed pump 109, part of the liquid returns to a forced circulation evaporation system, part of the liquid enters a second-stage flash separator 110 to be subjected to low-temperature flash evaporation, and the liquid reaches a certain concentration and enters a first sodium chloride thickener 111 and then enters a first sodium chloride centrifuge 112 to centrifuge out sodium chloride. The liquid from the first sodium chloride centrifuge 112 reaches a first mother liquor chloride tank 113 and is returned to the first stage separator 105 by a mother liquor chloride pump 111. And part of mother liquor discharged from the first sodium chloride mother liquor tank 113 is sent to a filter liquor concentrated liquor evaporation system to evaporate and separate sodium chloride and sodium nitrate. The nanofiltration clear liquid adopts two-stage evaporation crystallization and one-stage freezing crystallization processes, and the flow direction of the system materials is as follows: the raw material liquid enters the forced heater 202 for heating after passing through the second feeding pump 201, and then enters the forced separator 205 after passing through the second circulating pump 203, the secondary steam is pressurized by the second compressor 204 and then returns to the forced heater 202 for heating again, the heated material is evaporated and concentrated in the forced separator 205, the material containing part of crystals enters the single-effect evaporation separator 206 for high-temperature evaporation, then enters the second sodium chloride thickener 207, and then enters the second sodium chloride centrifuge 208 for centrifuging to obtain sodium chloride. The liquid in the second sodium chloride centrifuge 208 reaches a second sodium chloride mother liquor tank 209, then enters a cooling thickener 212 through a sodium chloride mother liquor pump 211, and then enters a sodium nitrate centrifuge 213 to centrifuge out sodium nitrate. The liquid from the sodium nitrate centrifuge 213 reaches a sodium nitrate mother liquor tank 214, and is returned to the single-effect evaporation separator 206 through a sodium nitrate mother liquor pump 215, and the crystallized sodium chloride is evaporated at high temperature.
After the technical scheme is adopted, the utility model discloses beneficial effect does: the utility model provides a coal chemical industry high salt waste water evaporation crystallization divides salt device, this system adopt receive and strain, evaporate, three kinds of modes of freezing carry out comprehensive treatment, three kinds of compositions of sodium nitrate, sodium chloride, the sodium sulfate that the recovery waste water contains. The system can better control the concentration and the proportion of each component in the evaporation process, so that the concentration and the proportion deviate from a common saturation curve to carry out evaporation crystallization, and the purity of the crystallized salt is greatly improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without inventive exercise.
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic structural diagram of the primary separator of the present invention.
Fig. 3 is a schematic structural diagram of the sodium sulfate centrifuge of the present invention.
Fig. 4 is a schematic structural diagram of the two-stage flash separator of the present invention.
Fig. 5 is a schematic diagram of the structure of the forced separator of the present invention.
Fig. 6 is a schematic structural view of the single-effect evaporation separator of the present invention.
Fig. 7 is a schematic structural view of the sodium nitrate centrifuge of the present invention.
Description of reference numerals: a first feeding pump 101, a first heater 102, a first circulating pump 103, a first-stage separator 105, a sodium sulfate thickener 106, a sodium sulfate centrifuge 107, a sodium sulfate mother liquor tank 108, a single-effect feeding pump 109, a second-stage flash separator 110, a first sodium chloride thickener 111, a first sodium chloride centrifuge 112, a first sodium chloride mother liquor tank 113, a second feeding pump 201, a forced heater 202, a second circulating pump 203, a forced separator 205, a single-effect evaporation separator 206, a second sodium chloride thickener 207, a second sodium chloride centrifuge 208, a second sodium chloride mother liquor tank 209, a sodium chloride mother liquor pump 211, a cooling thickener 212, a sodium nitrate centrifuge 213, a sodium nitrate mother liquor tank 214, a sodium nitrate mother liquor pump 215, a first-stage separator gas phase outlet 1051, a first-stage separator liquid phase outlet 1052, a first compressor 104, a sodium sulfate crystal outlet 1071, a sodium sulfate liquid phase outlet 1072, a flash evaporator gas phase outlet 1101, a flash evaporator gas phase outlet, a single-phase evaporator pump, A first intercooler 114, a forced separator vapor outlet 2051, a forced separator liquid outlet 2052, a second compressor 204, an evaporator vapor outlet 2061, a second intercooler 210, a sodium nitrate crystal outlet 2131, and a sodium nitrate liquid outlet 2132.
Detailed Description
Referring to fig. 1 to 7, the technical solution adopted by the present embodiment is: a device for separating salt from high-salinity wastewater in coal chemical industry through evaporative crystallization comprises a first feeding pump 101, wherein the output end of the first feeding pump 101 is connected with a first heater 102 through a pipeline, the output end of the first heater 102 is connected with a first circulating pump 103 through a pipeline, the output end of the first circulating pump 103 is connected with a first-stage separator 105 through a pipeline, the output end of the first-stage separator 105 is connected with a sodium sulfate thickener 106 through a pipeline, the output end of the sodium sulfate thickener 106 is connected with a sodium sulfate centrifuge 107 through a pipeline, the output end of the sodium sulfate centrifuge 107 is connected with a sodium sulfate mother liquor tank 108 through a pipeline, the output end of the sodium sulfate mother liquor tank 108 is connected with a single-effect feeding pump 109 through a pipeline, the output end of the single-effect feeding pump 109 is connected with a second-stage flash separator 110 through a pipeline, and the output end of the second-stage flash separator 110 is connected with a first sodium chloride thickener 111 through a pipeline, the output end of the first sodium chloride thickener 111 is connected with a first sodium chloride centrifuge 112 through a pipeline, the output end of the first sodium chloride centrifuge 112 is connected with a first sodium chloride mother liquor tank 113 through a pipeline, the output end of the first sodium chloride mother liquor tank 113 is connected with a second feeding pump 201 through a pipeline, the output end of the second feeding pump 201 is connected with a forced heater 202 through a pipeline, the output end of the forced heater 202 is connected with a second circulating pump 203 through a pipeline, the output end of the second circulating pump 203 is connected with a forced separator 205 through a pipeline, the output end of the forced separator 205 is connected with a single-effect evaporation separator 206 through a pipeline, the output end of the single-effect evaporation separator 206 is connected with a second sodium chloride thickener 207 through a pipeline, the output end of the second sodium chloride thickener 207 is connected with a second sodium chloride centrifuge 208 through a pipeline, the output end of the second sodium chloride centrifuge 208 is connected with a second sodium chloride mother liquor tank 209 through a pipeline, the output of second sodium chloride mother liquor jar 209 has sodium chloride mother liquor pump 211 through the pipe connection, the output of sodium chloride mother liquor pump 211 has cooling stiff ware 212 through the pipe connection, the output of cooling stiff ware 212 has sodium nitrate centrifuge 213 through the pipe connection, sodium nitrate centrifuge 213's output has sodium nitrate mother liquor jar 214 through the pipe connection, the output of sodium nitrate mother liquor jar 214 has sodium nitrate mother liquor jar 215 through the pipe connection, the output of sodium nitrate mother liquor jar 215 passes through the pipeline and is connected with the material input of single-effect evaporation separator 206.
The first-stage separator 105 is provided with a first-stage separator gas-phase outlet 1051 and a first-stage separator liquid-phase outlet 1052, and the first-stage separator liquid-phase outlet 1052 is connected with the input end of the sodium sulfate thickener 106 through a pipeline.
The gas phase outlet 1051 of the first-stage separator is connected with a first compressor 104 through a pipeline, and the output end of the first compressor 104 is connected with the steam input end of the first heater 102 through a pipeline.
The sodium sulfate centrifuge 107 is provided with a sodium sulfate crystal outlet 1071 and a sodium sulfate liquid phase outlet 1072, and the sodium sulfate liquid phase outlet 1072 is connected with the input end of a sodium sulfate mother liquor tank 108 through a pipeline.
The secondary flash evaporation separator 110 is provided with a flash evaporator gas phase outlet 1101, the flash evaporator gas phase outlet 1101 is connected with the first intercooler 114 through a pipeline, and the secondary steam after flash evaporation is fully cooled through the first intercooler 114.
The forced separator 205 is provided with a gas phase outlet 2051 and a liquid phase outlet 2052, and the liquid phase outlet 2052 is connected with the input end of the single-effect evaporation separator 206 through a pipeline.
The gas phase outlet 2051 of the forced separator is connected with a second compressor 204 through a pipeline, and the output end of the second compressor 204 is connected with the steam input end of the second heater 202 through a pipeline.
The single-effect evaporation separator 206 is provided with an evaporator gas-phase outlet 2061, the evaporator gas-phase outlet 2061 is connected with the second intercooler 210 through a pipeline, and the evaporated secondary steam is fully cooled by the second intercooler 210.
The sodium nitrate centrifuge 213 is provided with a sodium nitrate crystal outlet 2131 and a sodium nitrate liquid phase outlet 2132, and the sodium nitrate liquid phase outlet 2132 is connected with the input end of a sodium nitrate mother liquor tank 214 through a pipeline.
The utility model discloses a theory of operation: the flow direction of the nanofiltration concentrated solution evaporation crystallization salt separation material is as follows: the raw material liquid enters a first heater 102 for heating after passing through a first feeding pump 101, and then enters a first-stage separator 105 after passing through a first circulating pump 103, and secondary steam is pressurized by a compressor 4 and then returns to the first heater 102 again for heating. After the heated material is evaporated and concentrated in the first-stage separator 105, the material containing crystals enters a sodium sulfate thickener 106 and then enters a sodium sulfate centrifuge 107 to centrifuge out sodium sulfate, the liquid in the sodium sulfate centrifuge 107 reaches a sodium sulfate mother liquor tank 108 and then enters a single-effect feed pump 109, part of the liquid returns to a forced circulation evaporation system, part of the liquid enters a second-stage flash separator 110 to be subjected to low-temperature flash evaporation, and the liquid reaches a certain concentration and enters a first sodium chloride thickener 111 and then enters a first sodium chloride centrifuge 112 to centrifuge out sodium chloride. The liquid from the first sodium chloride centrifuge 112 passes to a first mother liquor chloride tank 113 and is returned to the first separator 105 by a mother liquor chloride pump 111. And part of mother liquor discharged from the first sodium chloride mother liquor tank 113 is sent to a filter liquor concentrated liquor evaporation system to evaporate and separate sodium chloride and sodium nitrate. The nanofiltration clear liquid adopts two-stage evaporation crystallization and one-stage freezing crystallization processes, and the flow direction of the system materials is as follows: the raw material liquid enters the forced heater 202 for heating after passing through the second feeding pump 201, and then enters the forced separator 205 after passing through the second circulating pump 203, the secondary steam is pressurized by the second compressor 204 and then returns to the forced heater 202 for heating again, the heated material is evaporated and concentrated in the forced separator 205, the material containing part of crystals enters the single-effect evaporation separator 206 for high-temperature evaporation, then enters the second sodium chloride thickener 207, and then enters the second sodium chloride centrifuge 208 for centrifuging to obtain sodium chloride. The liquid in the second sodium chloride centrifuge 208 reaches a second sodium chloride mother liquor tank 209, then enters a cooling thickener 212 through a sodium chloride mother liquor pump 211, and then enters a sodium nitrate centrifuge 213 to centrifuge out sodium nitrate. The liquid from the sodium nitrate centrifuge 213 reaches a sodium nitrate mother liquor tank 214, and is returned to the single-effect evaporation separator 206 through a sodium nitrate mother liquor pump 215, and the crystallized sodium chloride is evaporated at high temperature.
After the technical scheme is adopted, the utility model discloses beneficial effect does: the utility model provides a coal chemical industry high salt waste water evaporation crystallization divides salt device, this system adopt receive and strain, evaporate, three kinds of modes of freezing carry out comprehensive treatment, three kinds of compositions of sodium nitrate, sodium chloride, the sodium sulfate that the recovery waste water contains. The system can better control the concentration and the proportion of each component in the evaporation process, so that the concentration and the proportion deviate from a common saturation curve to carry out evaporation crystallization, and the purity of the crystallized salt is greatly improved.
The above description is only for the purpose of illustrating the technical solutions of the present invention and not for the purpose of limiting the same, and other modifications or equivalent replacements made by those of ordinary skill in the art to the technical solutions of the present invention should be covered within the scope of the claims of the present invention as long as they do not depart from the spirit and scope of the technical solutions of the present invention.
Claims (9)
1. The utility model provides a high salt waste water evaporation crystallization of coal industry divides salt device which characterized in that: the device comprises a first feeding pump (101), the output end of the first feeding pump (101) is connected with a first heater (102) through a pipeline, the output end of the first heater (102) is connected with a first circulating pump (103) through a pipeline, the output end of the first circulating pump (103) is connected with a first-stage separator (105) through a pipeline, the output end of the first-stage separator (105) is connected with a sodium sulfate thickener (106) through a pipeline, the output end of the sodium sulfate thickener (106) is connected with a sodium sulfate centrifugal machine (107) through a pipeline, the output end of the sodium sulfate centrifugal machine (107) is connected with a sodium sulfate mother liquor tank (108) through a pipeline, the output end of the sodium sulfate mother liquor tank (108) is connected with a single-effect feeding pump (109) through a pipeline, the output end of the single-effect feeding pump (109) is connected with a second-stage flash separator (110) through a pipeline, the output end of the second-stage flash separator (110) is connected with a first sodium chloride thickener (111) through a pipeline, the output end of the first sodium chloride thickener (111) is connected with a first sodium chloride centrifuge (112) through a pipeline, the output end of the first sodium chloride centrifuge (112) is connected with a first sodium chloride mother liquor tank (113) through a pipeline, the output end of the first sodium chloride mother liquor tank (113) is connected with a second feeding pump (201) through a pipeline, the output end of the second feeding pump (201) is connected with a forced heater (202) through a pipeline, the output end of the forced heater (202) is connected with a second circulating pump (203) through a pipeline, the output end of the second circulating pump (203) is connected with a forced separator (205) through a pipeline, the output end of the forced separator (205) is connected with a single-effect evaporation separator (206) through a pipeline, the output end of the single-effect evaporation separator (206) is connected with a second sodium chloride thickener (207) through a pipeline, the output end of the second sodium chloride thickener (207) is connected with a second sodium chloride centrifuge (208) through a pipeline, the output of second sodium chloride centrifuge (208) has second sodium chloride mother liquor jar (209) through the pipe connection, the output of second sodium chloride mother liquor jar (209) has sodium chloride mother liquor pump (211) through the pipe connection, the output of sodium chloride mother liquor pump (211) has cooling stiff ware (212) through the pipe connection, the output of cooling stiff ware (212) has sodium nitrate centrifuge (213) through the pipe connection, the output of sodium nitrate centrifuge (213) has sodium nitrate mother liquor jar (214) through the pipe connection, the output of sodium nitrate mother liquor jar (214) has sodium nitrate mother liquor pump (215) through the pipe connection, the output of sodium nitrate mother liquor pump (215) passes through the pipeline and is connected with the material input of single-effect evaporative separator (206).
2. The evaporation, crystallization and salt separation device for the high-salinity wastewater in the coal chemical industry according to claim 1, characterized in that: the first-stage separator (105) is provided with a first-stage separator gas-phase outlet (1051) and a first-stage separator liquid-phase outlet (1052), and the first-stage separator liquid-phase outlet (1052) is connected with the input end of the sodium sulfate thickener (106) through a pipeline.
3. The evaporation, crystallization and salt separation device for the high-salinity wastewater in the coal chemical industry according to claim 2, characterized in that: the gas phase outlet (1051) of the first-stage separator is connected with a first compressor (104) through a pipeline, and the output end of the first compressor (104) is connected with the steam input end of the first heater (102) through a pipeline.
4. The evaporation, crystallization and salt separation device for the high-salinity wastewater in the coal chemical industry according to claim 1, characterized in that: the sodium sulfate centrifuge (107) is provided with a sodium sulfate crystal outlet (1071) and a sodium sulfate liquid phase outlet (1072), and the sodium sulfate liquid phase outlet (1072) is connected with the input end of a sodium sulfate mother liquor tank (108) through a pipeline.
5. The evaporation, crystallization and salt separation device for the high-salinity wastewater in the coal chemical industry according to claim 1, characterized in that: the secondary flash evaporation separator (110) is provided with a flash evaporator gas phase outlet (1101), the flash evaporator gas phase outlet (1101) is connected with a first intercooler (114) through a pipeline, and the secondary steam after flash evaporation is fully cooled through the first intercooler (114).
6. The evaporation, crystallization and salt separation device for the high-salinity wastewater in the coal chemical industry according to claim 1, characterized in that: and a gas phase outlet (2051) and a liquid phase outlet (2052) of the forced separator are arranged on the forced separator (205), and the liquid phase outlet (2052) of the forced separator is connected with the input end of the single-effect evaporation separator (206) through a pipeline.
7. The evaporation, crystallization and salt separation device for the high-salinity wastewater in the coal chemical industry according to claim 6, characterized in that: the gas phase outlet (2051) of the forced separator is connected with a second compressor (204) through a pipeline, and the output end of the second compressor (204) is connected with the steam input end of the forced heater (202) through a pipeline.
8. The evaporation, crystallization and salt separation device for the high-salinity wastewater in the coal chemical industry according to claim 1, characterized in that: the single-effect evaporation separator (206) is provided with an evaporator gas-phase outlet (2061), the evaporator gas-phase outlet (2061) is connected with a second intercooler (210) through a pipeline, and the evaporated secondary steam is fully cooled by the second intercooler (210).
9. The coal chemical industry high salt waste water evaporation crystallization salt separating device of claim 1, characterized in that: the sodium nitrate centrifuge (213) is provided with a sodium nitrate crystal outlet (2131) and a sodium nitrate liquid phase outlet (2132), and the sodium nitrate liquid phase outlet (2132) is connected with the input end of a sodium nitrate mother liquor tank (214) through a pipeline.
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| CN202220708477.5U CN217103446U (en) | 2022-03-30 | 2022-03-30 | High salt waste water evaporation crystallization of coal industry divides salt device |
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