CN109179828B - Fluorine chemical plant sewage zero discharge and resource recovery method based on waste heat driving - Google Patents
Fluorine chemical plant sewage zero discharge and resource recovery method based on waste heat driving Download PDFInfo
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- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
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Abstract
A fluorine chemical plant sewage zero emission and resource recovery method based on waste heat driving belongs to the technical field of production process and sewage treatment of fluorine chemical plants such as polyvinylidene fluoride. Aiming at three types of sewage which are produced in large quantity in the production process of a related chemical plant and comprise process sewage containing recoverable materials, low-concentration sewage and high-concentration dangerous waste sewage, the invention respectively adopts different thermal method sewage recovery technologies based on waste heat driving, and comprises a cooling filtration purification device, a waste heat evaporation device and a crystallization device. The method uses the energy flow, water and sewage flow of the whole plant and the form and grade of the energy flow, water and sewage flow in different process sections to convert into the center, constructs an energy cascade comprehensive utilization system integrating energy conservation and environmental protection, and can realize zero discharge of sewage and cyclic utilization of resources of a chemical plant by using lower construction cost and greatly reducing manual energy consumption.
Description
Technical Field
The invention relates to a fluorine chemical plant sewage zero emission and resource recovery method based on waste heat driving, and belongs to the technical field of polyvinylidene fluoride and chemical production process and sewage treatment.
Background
The material flow and the energy flow in the existing polyvinylidene fluoride production generally comprise a plurality of flows: a pyrolysis preparation process of a vinylidene fluoride (VDF) tower kettle, a polymerization preparation process of a polyvinylidene fluoride (PVDF) tower kettle, a washing and press-filtering process, a drying granulation and packaging process, a sewage treatment process and the like, which are shown in fig. 1, wherein the main material flows are as follows: the material B used as the raw material → the VDF semi-finished product B1 prepared by the vinylidene fluoride column reactor device 5 → the PVDF semi-finished product B2 prepared by the polyvinylidene fluoride column reactor device 4 → the PVDF first-stage filter pressing state B3 obtained after the washing and filter pressing of the first-stage filter press 11 → the PVDF second-stage filter pressing state B4 obtained after the washing and filter pressing of the second-stage filter press 8 → the PVDF finished product B5 obtained after the drying and granulating device 15 is packaged.
The process water and sewage treatment process comprises the following steps: the method comprises the following steps of (1) heating source water (the daily consumption is about 2800t/d, the unit production water consumption is 200t/t) → ultrapure water making (about 1500t/d) → vinylidene fluoride tower kettle device 4, vinylidene fluoride tower kettle device 5 and steam heater 3, feeding the heated latter into a second-stage filter press 8 and a first-stage filter press 11 → collecting all drained water into a sewage treatment tank 12 for sewage treatment in a factory → discharging the qualified sewage to a local sewage treatment plant, and filling the sludge into a landfill or transporting the sludge outside.
The air flow of the drying process comprises the following steps: ambient air → air steam heater 14 → drying → granulating device 15 → venting to the atmosphere.
The main energy flows are (taking the productive energy consumption of 5000t/y designed capacity of a certain plant in one year as an example): the heat source steam A (the total steam consumption per day is about 200t/d, the energy consumption per unit production is reduced to 14.4t/t) of about 0.8MPa serving as a heat source is → the heating materials of the vinylidene fluoride tower kettle device 4 (the energy consumption is about 20t/d), the heating materials of the vinylidene fluoride tower kettle device 5 (the energy consumption is about 20t/d), the ultrapure water heating device 3 (the energy consumption is about 140t/d), and the inlet air for heating and drying of the air steam heater 14 (the energy consumption is about 20t/d) → the steam condensate water discharge. The refrigerating machines (two types of refrigerating machines, the outlet water temperature of a low-temperature refrigerating machine is-35 ℃, the COP1.256, the outlet water temperature of a normal-temperature refrigerating machine is 0 ℃, the COP3.42, and the total system running COP is about 1.5) → cold energy is input into the vinylidene fluoride tower kettle device 4 and the vinylidene fluoride tower kettle device 5 to cool materials → the cooling tower → the atmosphere, and the condenser cooling heat load → the process heat rejection and the compressor electric energy conversion is input into the cooling tower → the atmosphere.
Therefore, the material flow and the energy flow show that the polyvinylidene fluoride production needs to consume a large amount of high-temperature steam under the current situation, but a large amount of waste heat is lost, and the process and the cooling wastewater also discharge a large amount of sewage, so that the method belongs to the backward production process with high energy consumption, high pollution and high emission, and is seriously inconsistent with the requirements of the clean production era at the present with higher and higher energy-saving and environment-friendly requirements.
The method is characterized in that a large amount of three types of high-salt sewage are generated in the traditional production process of a fluorination plant such as polyvinylidene fluoride, the first type is process sewage containing recoverable materials generated in a filter pressing process section, the second type is low-concentration sewage containing desalted water concentrated water and cooling tower sewage, the third type is high-concentration dangerous waste sewage containing high-concentration process drainage water, acid-base neutralization water, regeneration waste water and secondary high-concentration water in a sewage treatment process, and in the current situation, steam evaporation, multiple-effect evaporation, MVR evaporation and the like are adopted to treat high-concentration residual sewage to realize zero sewage discharge, but the three types of high-salt sewage belong to technical methods with large investment and high energy consumption. According to the situation, Liu hong Xiang, xu tai zhi, Zhang hong and the like are used as patents of inventor applied in 24/03/2018, namely ' a polyvinylidene fluoride ultra-low energy consumption and sewage zero emission clean production process method ' (application number: 2018102480463) ' a polyvinylidene fluoride preparation process system based on ultra-low energy consumption ' (application number: 201820408016X) ', and a process method for realizing polyvinylidene fluoride ultra-low energy consumption and sewage zero emission clean production is designed.
Disclosure of Invention
The invention aims to solve the problems of high energy consumption, high pollution and high emission in the production of polyvinylidene fluoride in the prior art, and the method adopts a resource recovery device and a resource recovery system based on a thermal sewage zero emission technology to realize the recovery of the whole plant sewage resources including the second and third sewage resources and the content resources thereof, comprises the technical modes of adopting a special sewage heat exchange technology, a special salt separation purification technology, a special waste heat driven sewage evaporation concentration and crystallization technology and the like, and can be used for recovering waste heat resources and grade utilization energy resources in a step mode, recovering all process waste water in a plant and various materials and salts in the waste water and realizing the comprehensive recovery and cyclic utilization of the whole plant sewage resources, the material resources and more than 80 percent of process waste heat resources.
The specific description of the invention is: a fluorine chemical plant sewage zero discharge and resource recovery method based on waste heat driving aims at the large amount of three types of high-salinity sewage generated in the traditional production process of polyvinylidene fluoride, the first type is process sewage containing recoverable materials generated in a filter pressing process section, the second type is low-concentration sewage comprising desalted water concentrated water and cooling tower sewage, the third type is high-concentration dangerous waste sewage comprising process high-concentration drainage, acid-base neutralization water, regeneration wastewater and secondary high-concentration water in a sewage treatment process, it is characterized in that after low-concentration sewage P including concentrated desalted water and sewage discharged by a cooling tower passes through a pretreatment process section, the wastewater enters a high-concentration RO membrane 47 to generate clear water Q, and high-concentration wastewater of the high-concentration RO membrane 47 enters a multi-salt waste heat evaporation crystallizer 48 to generate wastewater secondary steam C2, industrial sodium chloride K3, industrial sodium sulfate K4 and miscellaneous salt K5; high-concentration dangerous waste sewage G including process high-concentration drainage, acid-base neutralization water, regeneration wastewater and secondary high-concentration water in a sewage treatment process enters a nanofiltration membrane salt separation device 44 after passing through a pretreatment process section, monovalent ion sewage of the nanofiltration membrane salt separation device 44 enters a single-salt waste heat evaporation crystallizer 45 again to generate sewage secondary steam C2 and industrial sodium chloride K3, high-valence ion sewage of the nanofiltration membrane salt separation device 44 enters a purification hardness removal device 46 again to be mixed with calcium oxide T1 and other chemical agents T2 to generate calcium sulfate K6 and miscellaneous salt K5, residual hardness-removal high-concentration sewage returns to a pre-oxidation device 40 to be subjected to circulation treatment, sewage secondary steam C2 generated by the single-salt waste heat evaporation crystallizer 45 and the multi-salt waste heat evaporation crystallizer 48 is connected with a heating side inlet of a primary waste heat heater 21, and clean water Q of the primary waste heat heater 21, an RO membrane 42 and a clean water high-concentration RO membrane 47 are sent to a water source water inlet of a brine removal device 32 and are communicated with a water source S The ultrapure water C outlet of the desalter 32 is connected with the heated side inlet of the first-stage waste heat heater 21, the heated side outlet of the first-stage waste heat heater 21 passes through the heated side of the second-stage waste heat heater 22 and then is connected with the heated side inlet of the high-temperature waste heat heater 31, the heated side outlet of the high-temperature waste heat heater 31 is connected with the heated side inlet of the steam heater 3, the heating side inlet of the second-stage waste heat heater 22 is connected with the outlet of the drainage water storage tank 10 and the high-temperature filter pressing water J1 of the first-stage filter press 11, the heating side outlet of the second-stage waste heat heater 22 is connected with the inlet of the evaporator of the filter pressing waste heat pump 23, the outlet of the evaporator is connected with the inlet of the low-temperature pressure water filtering J2 of the sewage treatment tank 12, the steam inlet of the generator of the filter pressing waste heat pump 23 is communicated with the steam outlet from the steam distributing cylinder 1, and the steam condensate D outlet of the generator is communicated, the outlet of the steam condensate water collecting device 24 is respectively communicated with the driving heat source inlets of the single-salt waste heat evaporating crystallizer 45 and the multi-salt waste heat evaporating crystallizer 48, after the driving heat source outlets of the single-salt waste heat evaporating crystallizer 45 and the multi-salt waste heat evaporating crystallizer 48 are connected, the outlet of the heating side of the second-stage air preheater 27 is connected with the outlet of the low-concentration sewage P, the inlet of the heating side of the second-stage air preheater 27 and the inlet of the heating side of the high-temperature waste heat heater 31, and then connected with the heated side of the condenser and the heated side of the absorber of the waste heat pump 23 for filter pressing, the heated side of the condenser and the heated side of the absorber are connected with the waste heat water inlet of the steam condensate water collecting device 24, and the steam condensate water inlet of the steam condensate water collecting device 24 is communicated with the outlets of the steam condensate water D generated by all process equipment including the steam condensate water D of the generator of the waste heat pump 23.
The primary waste heat heater 21 adopts a steam type heater structure, the secondary waste heat heater 22 adopts a special sewage heat exchanger structure, and the high-temperature waste heat heater 31 adopts plate exchange.
The residual heat pump 23 for filter pressing adopts a sewage-type absorption heat pump or a split-type injection heat pump structure.
The single salt waste heat evaporation crystallizer 45 adopts a negative pressure two-stage evaporation heat exchange structure.
The multi-salt waste heat evaporation crystallizer 48 adopts a negative pressure primary evaporation heat exchange structure.
The heating side of the secondary air preheater 27 and the heating side of the high-temperature waste heat heater 31 are connected in parallel, rather than in series.
The pretreatment process section for low-concentration sewage P comprises the following steps: a preliminary filtering and purifying device 41, an RO membrane 42, a sewage re-purifying device 43, or a pre-oxidation device 40 is additionally arranged before the preliminary filtering and purifying device 41.
The pretreatment process section for the high-concentration dangerous waste sewage G comprises the following steps: the pre-oxidation device 40, the preliminary filtering and purifying device 41, the RO membrane 42, the sewage re-purification device 43, or the pre-oxidation device 40 is eliminated.
The invention solves the problem of comprehensive recycling of waste heat resources, water resources, material resources and the like in polyvinylidene fluoride production, can realize the recovery rate of the waste heat resources to 80 percent, realizes comprehensive recovery, zero sewage discharge, material resource separation and recovery and can realize full resource utilization and the like for three types of sewage with different properties by adopting different technical modes, wherein compared with the conventional technology for zero sewage discharge and purification and recovery of hazardous waste salt, the invention can reduce the artificial energy requirement by about 90 percent, greatly reduce the energy consumption and reduce the operation cost by one order of magnitude, thereby becoming a brand new technical mode of comprehensive sewage treatment and resource recovery built and used by most industrial users. The invention can realize the mode conversion of the polyvinylidene fluoride preparation process from the high-energy consumption high-pollution high-emission industry to the clean production type green chemical plant with zero emission of process sewage and extremely low energy consumption and water resource consumption, and has technical, economic value, environmental protection and social effect.
Meanwhile, the technical method, the device and the engineering implementation scheme designed by the invention can be further popularized to similar process treatment processes of other industries, and have more general industrial application value and social and economic benefits.
Drawings
Fig. 1 is a schematic view of a conventional process system according to the present invention, and fig. 2 is a schematic view of the system according to the present invention.
The numbering and naming of the various components in FIGS. 1 and 2 are as follows.
A steam-separating cylinder 1, an ultrapure water tank 2, a steam heater 3, a polyvinylidene fluoride tower kettle device 4, a vinylidene fluoride tower kettle device 5, a process refrigerator 6, an evaporator 61, a condenser 62, an ultrapure water storage tank 7, a secondary filter press 8, a cooling tower 9, a drainage water storage tank 10, a primary filter press 11, a sewage treatment tank 12, a fan 13, an air steam heater 14, a drying-granulating device 15, a primary waste heat heater 21, a secondary waste heat heater 22, a waste heat pump 23 for filter pressing, a steam condensate water collecting device 24, a primary air preheater 26, a secondary air preheater 27, an exhaust waste heat recoverer 28, a sewage total reuse device 29, a sludge separation and reuse device 30, a high-temperature waste heat heater 31, a desalted water device 32, an acid-alkali neutralization tank 33, a pre-oxidation device 40, a primary filtration and purification device 41, a nanofiltration membrane 42, a sewage re-purification device 43, a nanofiltration membrane 44, a, The system comprises a single-salt waste heat evaporation crystallizer 45, a purification and hardness removal device 46, a high-concentration RO membrane 47, a multi-salt waste heat evaporation crystallizer 48, heat source steam A, VDF semi-finished product B1, PVDF semi-finished product B2, PVDF primary filter pressing state B3, PVDF secondary filter pressing state B4, packed PVDF finished product B5, ultrapure water C, steam condensate D, inlet air E, exhaust air F, high-concentration hazardous waste type sewage G, sludge H, sewage treatment plant drainage J, high-temperature filter pressing water J1, low-temperature filter pressing water J2, paraffin K1, other materials K2, industrial sodium chloride K3, industrial sodium sulfate K4, miscellaneous salt K5, calcium sulfate K6, F waste heat outlet water L1, waste heat inlet water L2, acidic material liquid M, alkaline material liquid N, low-concentration type sewage P, clear water Q, water source water replenishing S, calcium oxide T1 and other chemical agents T2.
Detailed Description
Fig. 2 is a schematic diagram of the system of the present invention.
The specific embodiment of the invention is as follows: a fluorine chemical plant sewage zero emission and resource recovery method based on waste heat drive is adopted, and a fluorine chemical plant sewage zero emission and resource recovery method and a system based on waste heat drive are adopted, low-concentration sewage P including desalted water concentrated water and cooling tower sewage enters a high-concentration RO membrane 47 to generate clear water Q after passing through a pretreatment process section, high-concentration sewage of the high-concentration RO membrane 47 enters a multi-salt waste heat evaporation crystallizer 48 to generate sewage secondary steam C2, industrial sodium chloride K3, industrial sodium sulfate K4 and miscellaneous salt K5; high-concentration dangerous waste sewage G including process high-concentration drainage, acid-base neutralization water, regeneration wastewater and secondary high-concentration water in a sewage treatment process enters a nanofiltration membrane salt separation device 44 after passing through a pretreatment process section, monovalent ion sewage of the nanofiltration membrane salt separation device 44 enters a single-salt waste heat evaporation crystallizer 45 again to generate sewage secondary steam C2 and industrial sodium chloride K3, high-valence ion sewage of the nanofiltration membrane salt separation device 44 enters a purification hardness removal device 46 again to be mixed with calcium oxide T1 and other chemical agents T2 to generate calcium sulfate K6 and miscellaneous salt K5, residual hardness-removal high-concentration sewage returns to a pre-oxidation device 40 to be subjected to circulation treatment, sewage secondary steam C2 generated by the single-salt waste heat evaporation crystallizer 45 and the multi-salt waste heat evaporation crystallizer 48 is connected with a heating side inlet of a primary waste heat heater 21, and clean water Q of the primary waste heat heater 21, an RO membrane 42 and a clean water high-concentration RO membrane 47 are sent to a water source water inlet of a brine removal device 32 and are communicated with a water source S The ultrapure water C outlet of the desalter 32 is connected with the heated side inlet of the first-stage waste heat heater 21, the heated side outlet of the first-stage waste heat heater 21 passes through the heated side of the second-stage waste heat heater 22 and then is connected with the heated side inlet of the high-temperature waste heat heater 31, the heated side outlet of the high-temperature waste heat heater 31 is connected with the heated side inlet of the steam heater 3, the heating side inlet of the second-stage waste heat heater 22 is connected with the outlet of the drainage water storage tank 10 and the high-temperature filter pressing water J1 of the first-stage filter press 11, the heating side outlet of the second-stage waste heat heater 22 is connected with the inlet of the evaporator of the filter pressing waste heat pump 23, the outlet of the evaporator is connected with the inlet of the low-temperature pressure water filtering J2 of the sewage treatment tank 12, the steam inlet of the generator of the filter pressing waste heat pump 23 is communicated with the steam outlet from the steam distributing cylinder 1, and the steam condensate D outlet of the generator is communicated, the outlet of the steam condensate water collecting device 24 is respectively communicated with the driving heat source inlets of the single-salt waste heat evaporating crystallizer 45 and the multi-salt waste heat evaporating crystallizer 48, after the driving heat source outlets of the single-salt waste heat evaporating crystallizer 45 and the multi-salt waste heat evaporating crystallizer 48 are connected, the outlet of the heating side of the second-stage air preheater 27 is connected with the outlet of the low-concentration sewage P, the inlet of the heating side of the second-stage air preheater 27 and the inlet of the heating side of the high-temperature waste heat heater 31, and then connected with the heated side of the condenser and the heated side of the absorber of the waste heat pump 23 for filter pressing, the heated side of the condenser and the heated side of the absorber are connected with the waste heat water inlet of the steam condensate water collecting device 24, and the steam condensate water inlet of the steam condensate water collecting device 24 is communicated with the outlets of the steam condensate water D generated by all process equipment including the steam condensate water D of the generator of the waste heat pump 23.
The primary waste heat heater 21 adopts a steam type heater structure, the secondary waste heat heater 22 adopts a special sewage heat exchanger structure, and the high-temperature waste heat heater 31 adopts plate exchange.
The residual heat pump 23 for filter pressing adopts a sewage-type absorption heat pump or a split-type injection heat pump structure.
The single salt waste heat evaporation crystallizer 45 adopts a negative pressure two-stage evaporation heat exchange structure.
The multi-salt waste heat evaporation crystallizer 48 adopts a negative pressure primary evaporation heat exchange structure.
The heating side of the secondary air preheater 27 and the heating side of the high-temperature waste heat heater 31 are connected in parallel, rather than in series.
The pretreatment process section for low-concentration sewage P comprises the following steps: a preliminary filtering and purifying device 41, an RO membrane 42, a sewage re-purifying device 43, or a pre-oxidation device 40 is additionally arranged before the preliminary filtering and purifying device 41.
The pretreatment process section for the high-concentration dangerous waste sewage G comprises the following steps: the pre-oxidation device 40, the preliminary filtering and purifying device 41, the RO membrane 42, the sewage re-purification device 43, or the pre-oxidation device 40 is eliminated.
It should be noted that the present invention provides a method for solving the recycling problem of waste heat resources, water resources and material resources by using a heat exchange method, a waste heat recovery and cascade heating method, a waste heat evaporation and energy cascade utilization method, etc. the general solution may have different specific implementation measures and different structure specific implementation devices, the above specific implementation is only one of them, and any other similar simple deformation implementation, such as type selection, series-parallel connection and number change related to the type of the waste heat recovery heat exchanger; a vapor compression heat pump is adopted to replace an absorption heat pump or an injection heat pump, or the number of the heat pumps is changed; the waste heat and the heating object of the heat pump are changed; the mode that the afterheat adopts the afterheat with low pressure lower than 100 ℃, or adopts the afterheat type of positive pressure steam, smoke and the like with higher than atmospheric pressure, or only adopts the afterheat-driven evaporation mode to implement part but not all of the claims, or carries out other deformation modes and the like which can be thought of by common professionals, or applies the technical mode to similar application occasions of other chemical plants and other plants except the polyvinylidene fluoride production industry with the same or similar structures, and the like, all fall into the protection scope of the invention.
Claims (8)
1. A fluoride factory sewage zero emission and resource recovery method based on waste heat driving aims at the fact that a large amount of three types of high-salinity sewage are generated in the traditional production process of polyvinylidene fluoride, the first type is recyclable material type process sewage which is generated in a filter pressing process section, the second type is low-concentration sewage which comprises desalted water concentrated water and cooling tower sewage, the third type is high-concentration dangerous waste sewage which is mixed with process high-concentration drainage water, acid-base neutralized water, regenerated wastewater and secondary high-concentration water generated in a sewage treatment process, and the fluoride factory sewage is characterized in that the low-concentration sewage (P) which comprises desalted water concentrated water and cooling tower sewage enters a high-concentration RO membrane (47) to generate clear water (Q) after passing through a pretreatment process section, and the high-concentration sewage of the high-concentration RO membrane (47) enters a multi-salt evaporation waste heat crystallizer (48) to generate sewage secondary steam (C2) and industrial sodium chloride (K3), Technical grade sodium sulfate (K4) and miscellaneous salts (K5); high-concentration dangerous waste sewage (G) including secondary high-concentration water in the process of high-concentration drainage, acid-base neutralized water, regenerated wastewater and sewage treatment enters a nanofiltration membrane salt separation device (44) after passing through a pretreatment process section, monovalent ion sewage of the nanofiltration membrane salt separation device (44) enters a single-salt waste heat evaporation crystallizer (45) again and generates sewage secondary steam (C2) and industrial sodium chloride (K3), high-valence ion sewage of the nanofiltration membrane salt separation device (44) enters a purification hardness removal device (46) again and is mixed with calcium oxide (T1) and other chemical agents (T2) to generate calcium sulfate (K6) and miscellaneous salt (K5), residual hardness-removal high-concentration sewage returns to a preposed oxidation device (40) for circulation treatment, sewage secondary steam (C2) generated by the single-salt waste heat evaporation crystallizer (45) and a multi-salt waste heat evaporation crystallizer (48) is connected with a heating side waste heat inlet of a primary heater (21), clean water (Q) of the primary waste heat heater (21), the RO membrane (42) and the high-concentration RO membrane (47) is sent to a water source water inlet of a desalted water device (32) and is communicated with a water source water replenishing (S), an ultrapure water (C) outlet of the desalted water device (32) is connected with a heated side inlet of the primary waste heat heater (21), heated side outlet water of the primary waste heat heater (21) passes through a heated side of the secondary waste heat heater (22) and is connected with a heated side inlet of the high-temperature waste heat heater (31), a heated side outlet of the high-temperature waste heat heater (31) is connected with a heated side inlet of the steam heater (3), a heating side inlet of the secondary waste heat heater (22) is connected with a water discharging and storing tank (10) and an outlet of high-temperature pressure filtration water (J1) of the primary filter press (11), a heating side outlet of the secondary waste heat heater (22) is connected with an inlet of an evaporator of the waste heat pump (23) for pressure filtration, the outlet of the evaporator is connected with the inlet of low-temperature filter pressing water (J2) of the sewage treatment tank (12), the steam inlet of the generator of the waste heat pump (23) for filter pressing is communicated with the steam outlet from the steam distributing cylinder (1), the outlet of steam condensate (D) of the generator is communicated with the steam condensate inlet of the steam condensate water collecting device (24), the outlet of the steam condensate water collecting device (24) is respectively communicated with the driving heat source crystallizer inlets of the single-salt waste heat evaporation crystallizer (45) and the multi-salt waste heat evaporation crystallizer (48), the driving heat source outlets of the single-salt waste heat evaporation crystallizer (45) and the multi-salt waste heat evaporation crystallizer (48) are respectively connected with the outlet pipe of low-concentration sewage (P), the heating side inlet of the secondary air preheater (27) and the heating side inlet of the high-temperature waste heat heater (31), the heating side outlet of the secondary air preheater (27) is connected with the heating side outlet of the high-temperature waste heat heater (31) and then connected with the waste heat pump (23) for filter pressing ) The heated side inlets of the condenser and the absorber are connected, the heated side outlets of the condenser and the absorber are connected with the residual heat water inlet of the steam condensation water collecting device (24), and the steam condensation water inlet of the steam condensation water collecting device (24) is communicated with the outlets of the steam condensation water (D) generated by all process equipment including the steam condensation water (D) of the generator of the residual heat pump (23).
2. The waste heat-driven fluorine chemical plant sewage zero emission and resource recovery method according to claim 1, wherein the primary waste heat heater (21) adopts a steam type heater structure, the secondary waste heat heater (22) adopts a special sewage heat exchanger structure, and the high temperature waste heat heater (31) adopts plate exchange.
3. The fluorine chemical plant sewage zero emission and resource recovery method based on waste heat driving as claimed in claim 1, characterized in that the waste heat pump (23) for filter pressing adopts a sewage-type absorption heat pump or a split-type injection heat pump structure.
4. The waste heat-driven fluorine chemical plant sewage zero emission and resource recovery method according to claim 1, wherein the single salt waste heat evaporation crystallizer (45) adopts a negative pressure secondary evaporation heat exchange structure.
5. The waste heat-driven fluorine chemical plant sewage zero emission and resource recovery method according to claim 1, wherein the multi-salt waste heat evaporation crystallizer (48) adopts a negative pressure primary evaporation heat exchange structure.
6. The waste heat-driven fluorine chemical plant wastewater zero emission and resource recovery method according to claim 1, wherein the heating side of the secondary air preheater (27) and the heating side of the high temperature waste heat heater (31) are connected in parallel rather than in series.
7. The waste heat-driven fluorine chemical plant wastewater zero emission and resource recovery method according to claim 1, wherein the low concentration wastewater (P) is subjected to a pretreatment process section comprising: a preliminary filtering and purifying device (41), an RO membrane (42) and a sewage re-purifying device (43), or a preposed oxidation device (40) is additionally arranged in front of the preliminary filtering and purifying device (41).
8. The waste heat-driven fluorine chemical plant sewage zero emission and resource recovery method according to claim 1, wherein the high-concentration dangerous waste sewage (G) is subjected to a pretreatment process section comprising: a pre-oxidation device (40), a primary filtering and purifying device (41), an RO membrane (42), a sewage re-purifying device (43), or the pre-oxidation device (40) is eliminated.
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