CN209797670U

CN209797670U - Resource recovery device based on thermal method sewage zero discharge technology in fluorine chemical plant

Info

Publication number: CN209797670U
Application number: CN201821438992.6U
Authority: CN
Inventors: 李先庭; 张茂勇; 刘士刚; 刘洪祥; 石文星; 王宝龙; 陈炜; 许太治; 王学勇; 岑俊平
Original assignee: Beijing Qing Technology Research Institute Co Ltd Datian Energy Industry; Tsinghua University
Current assignee: Beijing Qing Technology Research Institute Co Ltd Datian Energy Industry; Tsinghua University
Priority date: 2018-09-03
Filing date: 2018-09-03
Publication date: 2019-12-17
Anticipated expiration: 2028-09-03

Abstract

A resource recovery device based on a thermal sewage zero discharge technology in a fluorine chemical plant belongs to the technical field of fluorine chemical production process technology such as polyvinylidene fluoride and sewage treatment. Aiming at three types of sewage which are generated in large quantity in related chemical production processes and comprise process sewage containing recoverable materials, low-concentration sewage and high-concentration dangerous waste sewage, the patent respectively adopts different thermal method sewage recovery technologies based on waste heat driving, and comprises a cooling filtering purification device, a waste heat evaporation and crystallization device, an energy cascade comprehensive utilization system integrating energy conservation and environmental protection is constructed by using energy flow, water and sewage flow of a whole plant and the form and grade conversion of the energy flow, the water and the sewage flow in different process sections as centers, the sewage is heated, evaporated and concentrated until crystallization is carried out by adopting the recovered process waste heat, the comprehensive recovery of energy, water resources and contained material resources is realized, the energy saving rate is as high as about 90%, and a green manufacturing technology system for realizing the zero discharge of the sewage of the chemical plant and the cyclic utilization of the resources is comprehensively constructed.

Description

Resource recovery device based on thermal method sewage zero discharge technology in fluorine chemical plant

Technical Field

The utility model relates to a resource recovery device based on thermal method sewage zero release technique in fluorine factory belongs to polyvinylidene fluoride and chemical production technology and sewage treatment technical field.

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 200 t/t) → ultrapure water making (about 1500 t/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 14.4 t/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 20 t/d), the heating materials of the vinylidene fluoride tower kettle device 5 (the energy consumption is about 20 t/d), the ultrapure water heating device 3 (the energy consumption is about 140 t/d), and the inlet air for heating and drying of the air steam heater 14 (the energy consumption is about 20 t/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.

SUMMERY OF THE UTILITY MODEL

The utility model aims at solving the problems of high energy consumption, high pollution and high emission in the current polyvinylidene fluoride production, the method is used for realizing the recovery of the whole plant sewage resources including the second type and the third type sewage resources and the content resources thereof, comprehensively planning and optimizing the material flow and the energy flow, and adopting the resource recovery device and the system based on the thermal method sewage zero emission technology, including adopting the special sewage heat exchange technology, the special salt purification technology, the special waste heat driven sewage evaporation concentration and the crystallization technology and other technical modes, recovering the waste heat resources and utilizing the energy grade in the step, recovering all the process waste water in the plant, and the various materials and salts in the waste water, and realizing the comprehensive recovery and the cyclic utilization of the whole plant sewage resources, the material resources and the process waste heat resources more than 80 percent.

The utility model discloses a concrete description is: a resource recovery device based on a thermal method sewage zero discharge technology in a fluorine chemical plant is characterized in that low-concentration sewage P including concentrated desalted water and sewage discharged by a cooling tower 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 waste heat evaporation crystallizer 48 to generate sewage secondary steam C2 and 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 pipe of the low-concentration drainage P, the heat source side inlet of the secondary air preheater 27 and the heating side inlet of the high-temperature waste heat heater 31 are respectively connected, the heat source 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 heated side inlets of the condenser and the absorber of the waste heat pump 23 for filter pressing, the heated side outlets of the condenser and 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: the primary filtration purification device 41, the RO membrane 42 and the sewage re-purification device 43, or a pre-oxidation device 40 is additionally arranged before the primary filtration purification device 41, or other treatment links and devices are additionally arranged in the pretreatment process section.

The pretreatment process section for the high-concentration dangerous waste sewage G comprises the following steps: the pre-oxidation device 40, the primary filtering and purifying device 41, the RO membrane 42 and the sewage re-purification device 43, or the pre-oxidation device 40 is eliminated, or other treatment links and devices are added in the pretreatment process section.

The utility model provides a waste heat resource in the polyvinylidene fluoride production, the water resource, comprehensive recycle's such as material resource problem, can realize that waste heat resource recovery rate reaches 80%, three types of sewage of different nature adopt different technical mode to realize comprehensive recovery and sewage zero release, material resource separation recovery, and can realize whole resource utilization etc., wherein compare with conventional sewage zero release and danger waste salt purification recovery technique, can reduce the artifical energy demand about 90%, can reduce an order of magnitude with the working costs when reducing the energy consumption by a wide margin, become most of industrial users and build, the brand-new technical mode of comprehensive sewage treatment and resource recovery who has used up. 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.

Simultaneously, the utility model discloses a technical method and device and engineering implementation scheme thereof also can further promote to the similar technology processing in other trades, have more general industry using value and social 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 neutralizing tank 33, an oxidation device 40, a primary filtration and purification device 41, an RO membrane 42, a sewage re-purification device 43, a nanofiltration membrane 44, a desalination, 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 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 drainage 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 utility model discloses a concrete embodiment as follows: a resource recovery device based on a thermal method sewage zero discharge technology in a fluorine chemical plant comprises a low-concentration sewage P including desalted water concentrated water and cooling tower sewage, a high-concentration RO membrane 47 and a clear water Q are fed after a pretreatment process section, the high-concentration sewage of the high-concentration RO membrane 47 is fed into 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 pipe of the low-concentration drainage P, the heat source side inlet of the secondary air preheater 27 and the heating side inlet of the high-temperature waste heat heater 31 are respectively connected, the heat source 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 heated side inlets of the condenser and the absorber of the waste heat pump 23 for filter pressing, the heated side outlets of the condenser and 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.

It should be noted that the present invention provides a method, a device and an integrated system for comprehensively solving the recycling problem of waste heat resources, water resources and material resources by using a heat exchange method, a waste heat recovery and step heating method, a waste heat evaporation and energy step utilization method, etc., and different specific implementation measures and specific implementation devices with different structures can be provided according to the overall solution, the specific implementation manner is only one of them, and any other similar simple deformation implementation manners, such as type selection, series-parallel connection manner 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 of using low-pressure waste heat with the waste heat lower than 100 ℃ or using waste heat of positive pressure steam, smoke and the like with the waste heat higher than the atmospheric pressure, or only using the evaporation mode driven by the waste heat to implement a part but not all of the claims, or performing other deformation modes and the like which can be thought of by common professionals, or applying 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, all fall into the protection scope of the utility model.

Claims

1. A resource recovery device based on a thermal sewage zero discharge technology in a fluorine chemical plant comprises a sewage pretreatment process section, an evaporation salt separation crystallization process section and a waste heat utilization process section, and is characterized in that the sewage pretreatment process section is provided with a primary filtering and purifying device (41) for respectively treating low-concentration sewage and high-concentration sewage, the primary filtering and purifying device (41) is provided with a water inlet, the water inlet of the primary filtering and purifying device (41) for treating the low-concentration sewage is communicated with a water supply pipe of the low-concentration sewage (P) comprising desalted water and cooling tower sewage, the water outlet of the primary filtering and purifying device (41) is connected with the water inlet of an RO membrane (42), the water outlet of the RO membrane (42) is connected with the water inlet of a sewage re-purifying device (43), the water outlet of the sewage re-purifying device (43) is connected with the water inlet of a high-concentration RO membrane (47), the high-concentration RO membrane (47) is provided with a clear water (Q) outlet and a high-concentration sewage outlet, the high-concentration sewage outlet of the high-concentration RO membrane (47) is connected with a high-concentration sewage inlet of the multi-salt waste heat evaporation crystallizer (48), and the multi-salt waste heat evaporation crystallizer (48) is also provided with outlets of sewage secondary steam (C2), industrial sodium chloride (K3), industrial sodium sulfate (K4) or miscellaneous salt (K5); the water inlet of a primary filtering and purifying device (41) for treating high-concentration sewage is connected with the water outlet of a pre-oxidation device (40), the water inlet of the pre-oxidation device (40) is communicated with a water supply pipe of high-concentration dangerous waste sewage (G) including process high-concentration drainage, acid-base neutralization water, regeneration wastewater and secondary high-concentration water in the sewage treatment process, the water outlet of a sewage re-purification device (43) for treating high-concentration sewage is connected with the water inlet of a nanofiltration membrane salt separation device (44), a monovalent ion sewage outlet of the nanofiltration membrane salt separation device (44) is connected with the water inlet of a single salt waste heat evaporation crystallizer (45), the single salt waste heat evaporation crystallizer (45) is provided with a sewage secondary steam (C2) and an outlet of industrial sodium chloride (K3), a high-valence ion sewage outlet of the nanofiltration membrane salt separation device (44) is connected with a high-valence ion sewage inlet of a purification and hardness removal device (46), the purification and hardness removal device (46) is also provided with a feed inlet of calcium oxide (T1), other chemical agents (T2), a discharge outlet of calcium sulfate (K6) and miscellaneous salt (K5), a hardness removal high-concentration sewage outlet of the purification and hardness removal device (46) is connected with a hardness removal high-concentration sewage inlet of the front oxidation device (40), 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 the primary waste heat 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 the desalting device (32) and is communicated with water source replenishing water (S), an ultrapure water (C) outlet of the desalting device (32) is connected with a heated side inlet of the primary waste heat heater (21), and outlet water of the heated side of the primary waste heat heater (21) passes through a heated side of the secondary waste heat heater (22) and then is heated, the outlet of the heated side of the high-temperature waste heat heater (31) is connected with the inlet of the heated side of the steam heater (3), the inlet of the heated side 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 outlet of the heating side of the second-stage waste heat heater (22) is connected with the inlet of the evaporator of the waste heat pump (23) for filter pressing, the outlet of the evaporator is connected with the inlet of the low-temperature filter pressing water (J2) of the sewage treatment pool (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 steam condensate (D) outlet of the generator is communicated with the steam condensate inlet of the steam condensate water collecting device (24), and the outlet of the steam condensate water collecting device (24) is respectively connected with the single-salt evaporation waste heat crystallizer (45) and the multi-salt waste heat evaporation crystallizer (4) 48) The driving heat source inlet of the single salt waste heat evaporating crystallizer (45) is communicated with the driving heat source outlet of the multi-salt waste heat evaporating crystallizer (48), the outlet pipe of the low-concentration sewage (P), the heat source side inlet of the secondary air preheater (27) and the heating side inlet of the high-temperature waste heat heater (31) are respectively connected, the heat source 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 is connected with the condenser of the waste heat pump (23) for filter pressing and the heated side inlet of the absorber, the heated side outlets of the condenser and 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 steam condensate water (D) generated by all process equipment including the steam condensate water (D) of the generator of the waste heat pump (23).

2. The resource recovery device based on the thermal sewage zero emission technology in the fluorine chemical plant 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 resource recovery device based on the thermal sewage zero emission technology in the fluorine chemical plant according to claim 1, wherein the filter-pressing waste heat pump (23) adopts a sewage-type absorption heat pump or a split-type injection heat pump structure.

4. The resource recovery device based on the thermal sewage zero discharge technology in the fluorine chemical plant according to claim 1, wherein the single salt waste heat evaporation crystallizer (45) adopts a negative pressure secondary evaporation heat exchange structure.

5. The resource recovery device based on the thermal sewage zero discharge technology in the fluorine chemical plant according to claim 1, wherein the multi-salt waste heat evaporation crystallizer (48) adopts a negative pressure primary evaporation heat exchange structure.

6. The resource recovery device based on the thermal sewage zero emission technology in the fluorine chemical plant 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 resource recovery device based on the thermal wastewater zero emission technology in the fluorine chemical plant according to claim 1, wherein the pretreatment process section to which the low concentration wastewater (P) is subjected comprises: 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), or an ultrafiltration or nanofiltration treatment link and device are additionally arranged in a pretreatment process section.

8. The resource recovery device based on thermal wastewater zero emission technology in fluorine chemical plant according to claim 1, wherein the pretreatment process section for the high-concentration dangerous wastewater (G) comprises: a pre-oxidation device (40), a primary filtration purification device (41), an RO membrane (42) and a sewage re-purification device (43), or the pre-oxidation device (40) is cancelled, or the ultrafiltration or nanofiltration treatment link and device are added in the pretreatment process section.