CN209583869U - A waste water zero discharge and resource recovery system driven by thermal power plant waste heat - Google Patents

Abstract

A kind of sewage zero-discharge and resource recovering system based on the driving of steam power plant's waste heat, belongs to industrial energy saving and environmental protection technical field.The utility model total system includes four big processing FMEAs, that is thermal method waste water control and recycling plate, demineralized water plate, boiler and recuperation of heat plate, steam turbine power generation and waste heat recycle plate, driving heat source using a variety of residual heat resources as sewage evaporation and crystallization apparatus, steam power plant and external public sewage are realized and be concentrated by evaporation decrement, thermal method evaporation and high-purity divide salt, wherein for heating oxygen-eliminating device, the relatively high-grade steam or high-temperature water or fume high-temperature section sensible heat etc. of process water and heat supply network return water etc. are used for waste heat evaporative crystallization, purification and mother liquor desiccation, sewage side secondary steam residual heat recovery is preheated in heating target；Turbine condenser waste heat and fume afterheat are then used for negative pressure waste heat evaporation and concentration, and the clear water of recycling can be used for the moisturizing of demineralized water water source, and sodium chloride is used as the raw material of chlor-alkali plant etc., and calcium sulfate etc. can make construction material.

Description

A waste water zero discharge and resource recovery system driven by thermal power plant waste heat

technical field

The utility model relates to a sewage zero discharge and resource recovery system driven by waste heat of a thermal power plant, which belongs to the technical field of industrial energy saving and environmental protection.

Background technique

At present, most industries including thermal power plants or heat source plants need to discharge a large amount of sewage, especially industrial high-salt wastewater, which seriously pollutes the environment, especially the pollution of underground soil and groundwater resources, which is extremely difficult to recover. Although there are social voices, policy expectations and enterprise attempts to universally implement zero discharge of sewage and water resource reuse, the current conventional treatment methods, including the technical route of pretreatment + membrane treatment + MVR evaporation or multi-effect evaporation, exist. The biggest problem is: the initial investment is huge (at present, the investment demand for a ton of sewage, which is usually equivalent to 1t/h, is about 300,000 to 1 million yuan), and the operating energy consumption and operation and maintenance costs are too high (currently, it is usually equivalent to 30 to 90 yuan per ton of sewage treatment. At the same time, a large amount of waste salt and other solids discharged during the process of achieving zero sewage discharge are usually treated as hazardous waste, which must be disposed of in accordance with legal regulations, including disposal fees, environmental protection taxes The total comprehensive disposal cost, including the cost, is about 4,000-8,000 yuan/t. Therefore, whether it is zero sewage discharge or waste salt disposal, etc., the comprehensive investment and operation and maintenance costs are high. If the whole society starts to implement and strictly enforce it, the general view in the industry is that most industries with more sewage discharge Enterprises will be forced to stop production and go bankrupt.

Therefore, many companies in similar industries and policy choices are faced with a dilemma—whether they want "golden mountains and silver mountains" or "green water and green mountains"; One possible technical approach is to use waste heat from industrial enterprises such as thermal power plants to replace a large amount of high-grade energy that must be consumed in the process of zero sewage discharge and waste salt recycling as a driving heat source, which can greatly reduce its artificial energy consumption and At the same time, it can shorten the process of comprehensive sewage treatment and resource utilization, and through the efficient and optimized design of the heat exchange process, the heat exchange intensity can be improved, the consumption of heat exchange materials can be reduced, and the overall initial investment can be significantly reduced. According to the above-mentioned technical solutions, the analysis of the technical route by taking the thermal power plant as an example is as follows.

The boiler exhaust of thermal power plants or heat source plants is divided into higher temperature range (equivalent to 1% to 2% of the comprehensive thermal efficiency of thermal power plants) and low temperature range (equivalent to 9% to 12% of thermal power plant comprehensive thermal efficiency), both of which can provide a large amount of low-grade waste heat for use Evaporation, concentration and reduction of sewage; the exhaust steam condenser of the steam turbine can be installed with a low-vacuum circulating water heating method to provide a large amount of low-grade waste heat (equivalent to 20% to 60% of the comprehensive thermal efficiency of the thermal power plant) for the evaporation, concentration and reduction of sewage. Quantification; the water heating steam of the deaerator can provide a large amount of high-grade waste heat (equivalent to 5% to 9% of the comprehensive thermal efficiency of the thermal power plant) through energy cascade utilization for sewage evaporation concentration and reduction; central heating in winter The return water heating steam of the heating network can provide a large amount of high-grade waste heat (equivalent to 10% to 60% of the comprehensive thermal efficiency of the thermal power plant) through the energy cascade utilization method for the evaporation, concentration and reduction of sewage; if there is other process water that needs to be heated , then its influent heating steam can provide a large amount of high-grade waste heat (equivalent to 10% to 60% of the comprehensive thermal efficiency of the thermal power plant) through energy cascade utilization for sewage evaporation concentration and reduction. By utilizing the above waste heat heating and cascaded energy utilization methods, the heat that can usually be used for sewage evaporation and crystallization can reach 20% to 80% of the thermal efficiency of the thermal power plant, that is, the comprehensive heat utilization efficiency of the entire plant of the thermal power plant can even reach 110% to 170%. When adopting the above-mentioned waste heat utilization method for zero discharge of sewage, the incremental energy consumption is almost negligible except for the power consumption of the relevant water pumps, so the energy cost of the zero discharge of sewage is mainly the electricity cost for the operation of the water pumps in the process.

For example, if the average power consumption for ton of water treatment is 3-4kWh, and if the average on-grid electricity price of thermal power plants is 0.4 yuan/kWh, the energy cost for ton sewage treatment is only about 1.2-1.6 yuan/t. is 2.0-3.0 yuan/t; the comprehensive operating cost including other operation and maintenance costs is estimated to be about 3-6 yuan/t; compared with the comprehensive cost per ton of sewage zero discharge using conventional methods, it is an order of magnitude decline. This provides a technically and economically feasible technical basis for solving a large number of comprehensive sewage treatment problems and major social environmental protection problems generated by thermal power plants and more industries.

Utility model content

The purpose and task of this utility model is to carry out zero discharge of sewage, especially industrial high-salt wastewater produced in large quantities in the above-mentioned thermal power plants and enterprises in various industries, and to recycle water resources and content resources. Emission and resource recovery technology, through a variety of waste heat driven methods, conducts evaporation concentration reduction, thermal evaporation, salt separation, crystallization and purification of industrial sewage, and continuously circulates chloride ions, suspended solids, high-priced ions and heavy metals in it. Separation of water resources and contained material resources to achieve recovery of water resources and contained material resources. The recovered water resources can be transferred to the water supply of desalinated water production processes in thermal power plants and other factories, and water supply of heating network water, etc.; the recovered high-purity sodium chloride Used as raw materials for downstream factories such as chlor-alkali plants, and the recovered calcium sulfate can be used as building materials.

The specific description of the utility model is: a sewage zero discharge and resource recovery system driven by waste heat from a thermal power plant. The recovery block A3, the steam turbine power generation and waste heat recovery block A4, and the auxiliary pipeline facilities inside and between the blocks are characterized in that the condenser 42 of the steam turbine power generation and waste heat recovery block A4 adopts a low-vacuum heat exchange structure, and the boiler and heat recovery In addition to the boiler body 33 and its conventional auxiliary system, block A3 also includes a flue gas sewage evaporator 34 and a boiler flue gas waste heat recovery component 30 based on the boiler inlet air water vapor heat transfer cycle, thermal sewage treatment and resource utilization of block A1 The inlet of the desalted concentrated water P1 of the multimedia filter 1 is connected to the outlet of the desalted concentrated water P1 of the desalted water plate A2, and the inlet of the cooling tower sewage P2 of the multimedia filter 1 is connected to the steam turbine power generation and waste heat recovery plate A4 The outlet of the cooling tower sewage P2 of the cooling tower 44 is connected, the outlet of the suspended high-concentration water G9 of the multi-media filter 1 is connected with the raw water inlet of the flocculation sedimentation tank 21, and the press-filtered water inlet of the multi-media filter 1 is connected to the first press water inlet. The filter press water outlet of the filter 20 is connected, the treated water outlet of the multi-media filter 1 is connected with the raw water inlet of the first-stage reverse osmosis membrane 2, the outlet of the first-stage clean water D5 of the first-stage reverse osmosis membrane 2 is connected with the outlet of the desalted water plate A2 The inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23 is connected, the treated water outlet of the primary reverse osmosis membrane 2 is connected with the raw water inlet of the secondary reverse osmosis membrane 3, and the outlet of the secondary clear water D4 of the secondary reverse osmosis membrane 3 is connected with the The inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23 is connected, and the outlet of the treated water of the secondary reverse osmosis membrane 3 is connected with the inlet of the high-concentration raw water G of the mixed water pretreatment tank 4, and the import of the high-concentration raw water G is also separately included. From the primary reverse osmosis membrane 2, the secondary reverse osmosis membrane 3, the ultrafiltration/microfiltration membrane treatment device 6, the second filter press 15, the source water pretreatment pool 22 from the desalinated water plate A2, the desalted water reverse osmosis membrane 23. The outlet of the high-concentration drainage including the desulfurization tower 34 of the boiler and the heat recovery section A3 is connected, and the outlet of the high-concentration water G1 of the mixed water pretreatment tank 4 is connected to the raw water inlet of the second filter press 15, and the mixed water The treated water outlet of the pretreatment tank 4 is connected to the raw water inlet of the oxidized calcification tank 5, and the oxidized calcification tank 5 is provided with the inlet of the oxidant O, the feeding port of the lime milk and the compound agent F, the feeding port of the calcium sulfate K3, and other solid salts The outlet of K5, the outlet of treated water, the outlet of treated water in oxidized calcification tank 5 are connected with the raw water inlet of ultrafiltration/microfiltration membrane treatment device 6, and the ultrafiltration/microfiltration membrane treatment device 6 is provided with the feed of lye CH mouth, the outlet of regenerated sewage G3 and the treated water outlet, the treated water outlet of the ultrafiltration/microfiltration membrane treatment device 6 is connected with the raw water inlet of the nanofiltration membrane salt separation device 7, and the high concentration water H of the nanofiltration membrane salt separation device 7 The outlet of the oxidized calcification tank 5 is connected to the inlet of the high concentrated water H, the purified water outlet of the nanofiltration membrane salt separation device 7 is connected to the raw water inlet of the waste heat evaporation crystallizer 8, and the waste heat evaporation crystallizer 8 is provided with the inlet of the waste heat heat source J1 , waste heat heat source The outlet of water J2, the salt outlet of industrial grade sodium chloride K1, the outlet of sewage secondary steam L and the outlet of mother liquor G4, in which the outlet of sewage secondary steam L of waste heat evaporation crystallizer 8 and waste heat recovery unit 10+ 11 is connected to the high-temperature side inlet, the high-temperature side condensate outlet of the waste heat recovery unit 10+11 is connected to the inlet of the regenerated raw water D of the desalinated reverse osmosis membrane 23, and the treated water outlet of the ultrafiltration/microfiltration membrane treatment device 6 is also connected to The raw water inlet of the negative pressure waste heat evaporator 14 is connected, and the negative pressure waste heat evaporator 14 is provided with the inlet of the first low-temperature waste heat source R1, the outlet of the first low-temperature waste heat source water R2, the inlet of the second low-temperature waste heat source R3, the second low-temperature The outlet of waste heat heat source effluent R4, the outlet of low-pressure sewage secondary steam Ld and the outlet of low-pressure mother liquor G5, wherein the outlet of low-pressure mother liquor G5 is connected with the raw water inlet of mother liquor drying waste heat evaporator 13, and mother liquor drying waste heat evaporator 13 is provided with The inlet of the waste heat source J1, the outlet of the waste heat source water outlet J2, the outlet of the mother liquor drying solid waste K6, the outlet of the low-pressure sewage secondary steam Ld of the negative pressure waste heat evaporator 14, and the steam inlet of the circulating cooling water heat exchanger 12 Connected, the inlet of the cooling water N1 of the circulating cooling water heat exchanger 12 is connected with the cooling water outlet of the cooling tower 44, the cooling water outlet N2 of the circulating cooling water heat exchanger 12 is connected with the cooling water inlet of the cooling tower 44, and the circulation The outlet of the low-pressure clean water D3 of the cooling water heat exchanger 12 communicates with the inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23 .

The salt outlet of the industrial grade sodium chloride K1 of the waste heat evaporation crystallizer 8 communicates with the feed port of the crystallization salt repurification device 9, and the crystallization salt repurification device 9 is provided with the inlet of the waste heat heat source J1 and the outlet of the condensate return water J2 , High-purity industrial grade sodium chloride K4 outlet.

The inlet of the high-temperature exhaust gas Y of the flue gas and sewage evaporator 37 of the boiler and heat recovery section A3 is connected to the flue of the high-temperature exhaust Y from the boiler or dust collector, and the outlet of the medium-temperature flue gas Y0 of the flue gas and sewage evaporator 37 is connected to the The inlet of the desulfurization inlet smoke Y1 of the desulfurization tower 34 is connected, the inlet of the mother liquor G4 for spraying of the flue gas sewage evaporator 37 is connected with the outlet of the mother liquor G4 of the waste heat evaporation crystallizer 8, or the low-pressure mother liquor G5 of the negative pressure waste heat evaporator 14 The outlets of other high-concentration sewage and wastewater sources are connected, and the flue gas sewage evaporator 37 is also provided with a discharge port for flue gas drying and solid waste K7.

Boiler flue gas waste heat recovery component 30 includes boiler flue gas waste heat composite spray tower 31, the flue gas inlet of boiler flue gas waste heat composite spray tower 31 is connected with the outlet of desulfurization flue gas Y1 of desulfurization tower 34, boiler flue gas waste heat composite spray The outlet of the flue gas waste heat high-temperature water Rg1 of the shower tower 31 is connected to the inlet of the first low-temperature waste heat heat source R1 of the negative pressure waste heat evaporator 14, and the inlet of the flue gas waste heat low-temperature water Rh2 of the boiler flue gas waste heat composite spray tower 31 is connected to the first low-temperature waste heat source R1 of the negative pressure waste heat evaporator 14. The outlets of a low-temperature waste heat heat source effluent R2 are connected.

In addition to being connected to the cooling water inlet of the cooling tower 44, the outlet of the circulating water outlet Rg3 of the condenser 42 of the steam turbine power generation and waste heat recovery section A4 is also connected to the inlet of the second low-temperature waste heat heat source R3 of the negative pressure waste heat evaporator 14. The inlet of the circulating water inlet Rh4 of the condenser 42 is not only connected with the cooling water outlet of the cooling tower 44, but also connected with the outlet of the second low-temperature waste heat heat source outlet water R4.

The steam extraction outlet of the steam turbine 43 of the steam turbine power generation and waste heat recovery section A4 is in addition to the steam inlet of the feedwater heater assembly 40, the steam inlet of the deaerator 41, and the high temperature side inlet of the hot water heater 46 of the heating or process heat user. In addition to being connected, it also communicates with the inlet of the waste heat heat source J1 of the waste heat evaporation crystallizer 8, or communicates with the entrance of the waste heat heat source J1 of the crystallization salt repurification device 9, or communicates with the entrance of the waste heat heat source J1 of the mother liquor drying waste heat evaporator 13 , the condensed water inlet of the deaerator 41 is not only connected with the condensed water outlet of the condenser 42, the condensed water return water J2 outlet of the hot water heater 46, but also connected with the waste heat evaporation crystallizer 8, or crystallized salt repurification The device 9, the outlet of the condensate return water J2 of the mother liquor drying waste heat evaporator 13 communicates with the outlet of the deaerator in the waste heat recovery unit 10+11 and the heated effluent M2 of the process water waste heat heater 11, The inlet of the heated water M1 of the deaerator and process water waste heat heater 11 communicates with the condensed water outlet of the condenser 42 .

The waste heat recovery unit 10+11 includes the heat network return water waste heat heater 10, the inlet of the heat network return water inlet water M3 of the heat network return water waste heat heater 10 and the low temperature return water Rh of the hot water heater 46. The water pipes are connected, the outlet of the heat network return water inlet and outlet M4 of the heat network return water waste heat heater 10 is connected with the inlet of the low temperature return water Rh of the hot water heater 46, and the high temperature side inlet of the heat network return water waste heat heater 10 It is connected with the outlet of the sewage secondary steam L of the waste heat evaporation crystallizer 8, the outlet of the second drainage D2 on the high temperature side of the heat network return water waste heat heater 10 is connected with the first water discharge on the high temperature side of the deaerator and the process water waste heat heater 11 After the outlet of D1 is connected, it communicates with the inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23 .

The multi-media filter 1 of the thermal sewage treatment and resource utilization section A1 is also provided with an external concentrated water Pw inlet, which communicates with the water inlet pipeline of the low-concentration sewage source in the public sewage inflow outside the thermal power plant. The mixed water pretreatment tank 4 of the sewage treatment and resource utilization section A1 is also provided with an external high-concentration raw water Gw inlet, which communicates with the water inlet pipeline of the higher-concentration sewage source in the public sewage inflow outside the thermal power plant. The crystallized salt repurification device 9 of the sewage treatment and resource utilization section A1 is also provided with a feed port of the public external primary industrial salt Kw other than the thermal power plant.

The utility model solves the problem of low-cost comprehensive treatment and resource utilization of a large amount of sewage, especially high-salt wastewater produced in the production process of many industrial enterprises such as thermal power plants. High-purity industrial-grade sodium chloride, calcium sulfate and other resources are recovered, and at the same time, artificial energy consumption and operating costs are greatly saved. Among them, compared with conventional zero discharge of sewage and hazardous waste salt purification and recovery technology, it can reduce the artificial energy demand by about 90%, greatly reduce energy consumption and reduce operating costs by an order of magnitude, becoming the most built-in thermal power plants and related industrial users. A brand-new technical method of comprehensive sewage treatment and resource recovery that is affordable and affordable. The utility model can take thermal power plant and its power system technology and thermal process as the center, realize the transformation from high pollution and high discharge mode to clean production green power plant mode with zero discharge of process sewage and significantly reduced water resource consumption, especially as The basic technical process of the industrial park and even the whole society's integrated environmental protection system, the public environmental protection factory and the comprehensive treatment center that undertake the comprehensive treatment of public sewage, have both technical and economic value as well as environmental protection and social effects.

This method significantly reduces the energy consumption and cost of zero discharge of sewage and realizes efficient resource utilization. It is especially suitable for joint operation of thermal power plants or heat source plants and chlor-alkali processes, and can further improve the completeness of industrial facilities and technical and economic effects of comprehensive treatment. . At the same time, the technical method and its device and engineering implementation plan designed by the utility model can also be further extended to the comprehensive treatment of industrial enterprises with high energy consumption and high waste heat discharge in other industries, and even extended to other related hazardous waste treatment In the process, it has more general industrial application value and social and economic benefits.

Description of drawings

Fig. 1 is a schematic diagram of the system of the present utility model.

The numbers and names of the parts in Figure 1 are as follows. Multi-media filter 1, primary reverse osmosis membrane 2, secondary reverse osmosis membrane 3, mixed water pretreatment tank 4, oxidized calcification tank 5, ultrafiltration/microfiltration membrane treatment device 6, nanofiltration membrane salt separation device 7, Waste heat evaporation crystallizer 8, crystallization salt repurification device 9, heat network return water waste heat heater 10, deaerator and process water waste heat heater 11, circulating cooling water heat exchanger 12, mother liquor drying waste heat evaporator 13, negative Pressure waste heat evaporator 14, second filter press 15, first filter press 20, flocculation sedimentation tank 21, source water pretreatment tank 22, desalinated water reverse osmosis membrane 23, desalinated water advanced treatment device 24, boiler flue gas waste heat Recovery component 30, boiler flue gas waste heat composite spray tower 31, blower 32, boiler body 33, desulfurization tower 34, flue gas dust collector 35, induced draft fan 36, flue gas sewage evaporator 37, feed water heater assembly 40, oxygen removal Condenser 41, Condenser 42, Cooling Tower 44, Generator 45, Hot Water Heater 46, Thermal Sewage Treatment and Recycling Section A1, Desalted Water Section A2, Boiler and Heat Recovery Section A3, Steam Turbine Power Generation and Waste Heat Recovery Section A4, desulfurization circulating water B, lye CH, regenerated raw water D, high temperature side first drainage D1, high temperature side second drainage D2, low pressure clean water D3, secondary clean water D4, primary clean water D5, lime milk and compound agent F, High-concentration raw water G, sewage high-concentration water G1, desulfurization sewage G2, recycled sewage G3, mother liquor G4, low-pressure mother liquor G5, first-level membrane regeneration sewage G6, second-level membrane regeneration sewage G7, desalted water regeneration sewage G8, suspension high-concentration Water G9, external high-concentration raw water Gw, high-concentration water H, waste heat source J1, waste heat source water J2, industrial-grade sodium chloride K1, filter press sludge K2, calcium sulfate K3, high-purity industrial-grade sodium chloride K4, other solid salt K5, mother liquor drying solid waste K6, flue gas drying solid waste K7, public external primary industrial salt Kw, sewage secondary steam L, low-pressure sewage secondary steam Ld, heated water inlet M1, heated Outlet water M2, heating network return water inlet and incoming water M3, heating network return water inlet and outlet M4, cooling water inlet N1, cooling outlet water N2, oxidant O, desalinated concentrated water P1, cooling tower sewage P2, external concentrated water Pw, the first low-temperature waste heat source R1, the first low-temperature waste heat source water R2, the second low-temperature waste heat source R3, the second low-temperature waste heat source water R4, the high-temperature water supply Rh of the heating network, the low-temperature return water Rh, the flue gas waste heat high-temperature water Rg1, Flue gas waste heat low-temperature water Rh2, circulating water outlet Rg3, circulating water inlet Rh4, source water S, high-temperature smoke exhaust Y, medium-temperature flue gas Y0, desulfurization smoke inlet Y1, desulfurization smoke exhaust Y2, low-temperature smoke exhaust Y3.

Detailed ways

Fig. 1 is a schematic diagram of the system of the present utility model.

The specific implementation of the utility model is as follows: a sewage zero discharge and resource recovery system driven by the waste heat of a thermal power plant. The heat recovery block A3, the steam turbine power generation and waste heat recovery block A4, and the auxiliary pipeline facilities inside and between the blocks are characterized in that the condenser 42 of the steam turbine power generation and waste heat recovery block A4 adopts a low-vacuum heat exchange structure, and the boiler and heat In addition to the boiler body 33 and its conventional auxiliary system, the recovery section A3 also includes the flue gas sewage evaporator 34 and the boiler flue gas waste heat recovery component 30 based on the boiler inlet air water vapor heat transfer cycle, and the thermal sewage treatment and resource utilization section A1 The inlet of the desalted concentrated water P1 of the multimedia filter 1 is connected with the outlet of the desalted concentrated water P1 of the desalted water block A2, and the inlet of the cooling tower sewage P2 of the multimedia filter 1 is connected with the steam turbine power generation and waste heat recovery block A4 The outlet of the cooling tower blowdown water P2 of the cooling tower 44 is connected, the outlet of the suspended high-concentration water G9 of the multi-media filter 1 is connected with the raw water inlet of the flocculation sedimentation tank 21, and the press-filtered water inlet of the multi-media filter 1 is connected with the first The filter press water outlet of the filter press 20 is connected, the treated water outlet of the multi-media filter 1 is connected with the raw water inlet of the first-stage reverse osmosis membrane 2, and the outlet of the first-stage clear water D5 of the first-stage reverse osmosis membrane 2 is connected with the desalted water plate A2 The inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23 is connected, the treated water outlet of the first-stage reverse osmosis membrane 2 is connected with the raw water inlet of the second-stage reverse osmosis membrane 3, and the outlet of the second-stage clean water D4 of the second-stage reverse osmosis membrane 3 It is connected with the inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23, and the outlet of the treated water of the secondary reverse osmosis membrane 3 is connected with the inlet of the high-concentration raw water G of the mixed water pretreatment tank 4. Including primary reverse osmosis membrane 2, secondary reverse osmosis membrane 3, ultrafiltration/microfiltration membrane treatment device 6, second filter press 15, source water pretreatment pool 22 from desalted water plate A2, desalted water reverse osmosis Membrane 23 and the high-concentration drainage outlet including the desulfurization tower 34 from the boiler and heat recovery plate A3 are connected. The treated water outlet of the water pretreatment tank 4 is connected with the raw water inlet of the oxidized calcification tank 5, and the oxidized calcification tank 5 is provided with the inlet of the oxidant O, the feeding port of lime milk and compound agent F, the feeding port of calcium sulfate K3, and other solid The outlet of the salt K5, the outlet of the treated water, the outlet of the treated water of the oxidized calcification tank 5 is connected with the raw water inlet of the ultrafiltration/microfiltration membrane treatment device 6, and the ultrafiltration/microfiltration membrane treatment device 6 is provided with an inlet for lye CH The feed port, the outlet of the regenerated sewage G3 and the outlet of the treated water, the outlet of the treated water of the ultrafiltration/microfiltration membrane treatment device 6 is connected to the raw water inlet of the nanofiltration membrane salt separation device 7, and the high concentration water of the nanofiltration membrane salt separation device 7 The outlet of H is connected to the inlet of the high concentration water H of the oxidized calcification tank 5, the purified water outlet of the nanofiltration membrane salt separation device 7 is connected to the raw water inlet of the waste heat evaporation crystallizer 8, and the waste heat evaporation crystallizer 8 is provided with a waste heat heat source J1 Import, waste heat The outlet of source water J2, the salt outlet of industrial grade sodium chloride K1, the outlet of sewage secondary steam L and the outlet of mother liquor G4, wherein the outlet of sewage secondary steam L of waste heat evaporation crystallizer 8 and waste heat recovery unit 10 The high-temperature side inlet of +11 is connected, the condensed water outlet of the high-temperature side of the waste heat recovery unit 10+11 is connected with the inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23, and the treated water outlet of the ultrafiltration/microfiltration membrane treatment device 6 is also Connected with the raw water inlet of the negative pressure waste heat evaporator 14, the negative pressure waste heat evaporator 14 is provided with the inlet of the first low-temperature waste heat heat source R1, the outlet of the first low-temperature waste heat heat source outlet water R2, the inlet of the second low-temperature waste heat heat source R3, the second The outlet of the low-temperature waste heat heat source effluent R4, the outlet of the low-pressure sewage secondary steam Ld and the outlet of the low-pressure mother liquor G5, wherein the outlet of the low-pressure mother liquor G5 is connected to the raw water inlet of the mother liquor drying waste heat evaporator 13, and the mother liquor drying waste heat evaporator 13 is set There are the inlet of the waste heat source J1, the outlet of the waste heat source water outlet J2, the outlet of the mother liquor drying solid waste K6, the outlet of the low-pressure sewage secondary steam Ld of the negative pressure waste heat evaporator 14 and the steam of the circulating cooling water heat exchanger 12 The inlets are connected, the inlet of the cooling water N1 of the circulating cooling water heat exchanger 12 is connected with the cooling water outlet of the cooling tower 44, the outlet of the cooling water N2 of the circulating cooling water heat exchanger 12 is connected with the cooling water inlet of the cooling tower 44, The outlet of the low-pressure clean water D3 of the circulating cooling water heat exchanger 12 communicates with the inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23 .

The salt outlet of the industrial grade sodium chloride K1 of the waste heat evaporation crystallizer 8 communicates with the feed port of the crystallization salt repurification device 9, and the crystallization salt repurification device 9 is provided with the inlet of the waste heat heat source J1 and the outlet of the condensate return water J2 , High-purity industrial grade sodium chloride K4 outlet.

The inlet of the high-temperature exhaust gas Y of the flue gas and sewage evaporator 37 of the boiler and heat recovery section A3 is connected to the flue of the high-temperature exhaust Y from the boiler or dust collector, and the outlet of the medium-temperature flue gas Y0 of the flue gas and sewage evaporator 37 is connected to the The inlet of the desulfurization inlet smoke Y1 of the desulfurization tower 34 is connected, the inlet of the mother liquor G4 for spraying of the flue gas sewage evaporator 37 is connected with the outlet of the mother liquor G4 of the waste heat evaporation crystallizer 8, or the low-pressure mother liquor G5 of the negative pressure waste heat evaporator 14 The outlets of other high-concentration sewage and wastewater sources are connected, and the flue gas sewage evaporator 37 is also provided with a discharge port for flue gas drying and solid waste K7.

Boiler flue gas waste heat recovery component 30 includes boiler flue gas waste heat composite spray tower 31, the flue gas inlet of boiler flue gas waste heat composite spray tower 31 is connected with the outlet of desulfurization flue gas Y1 of desulfurization tower 34, boiler flue gas waste heat composite spray The outlet of the flue gas waste heat high-temperature water Rg1 of the shower tower 31 is connected to the inlet of the first low-temperature waste heat heat source R1 of the negative pressure waste heat evaporator 14, and the inlet of the flue gas waste heat low-temperature water Rh2 of the boiler flue gas waste heat composite spray tower 31 is connected to the first low-temperature waste heat source R1 of the negative pressure waste heat evaporator 14. The outlets of a low-temperature waste heat heat source effluent R2 are connected.

In addition to being connected to the cooling water inlet of the cooling tower 44, the outlet of the circulating water outlet Rg3 of the condenser 42 of the steam turbine power generation and waste heat recovery section A4 is also connected to the inlet of the second low-temperature waste heat heat source R3 of the negative pressure waste heat evaporator 14. The inlet of the circulating water inlet Rh4 of the condenser 42 is not only connected with the cooling water outlet of the cooling tower 44, but also connected with the outlet of the second low-temperature waste heat heat source outlet water R4.

The steam extraction outlet of the steam turbine 43 of the steam turbine power generation and waste heat recovery section A4 is in addition to the steam inlet of the feedwater heater assembly 40, the steam inlet of the deaerator 41, and the high temperature side inlet of the hot water heater 46 of the heating or process heat user. In addition to being connected, it also communicates with the inlet of the waste heat heat source J1 of the waste heat evaporation crystallizer 8, or communicates with the entrance of the waste heat heat source J1 of the crystallization salt repurification device 9, or communicates with the entrance of the waste heat heat source J1 of the mother liquor drying waste heat evaporator 13 , the condensed water inlet of the deaerator 41 is not only connected with the condensed water outlet of the condenser 42, the condensed water return water J2 outlet of the hot water heater 46, but also connected with the waste heat evaporation crystallizer 8, or crystallized salt repurification The device 9, the outlet of the condensate return water J2 of the mother liquor drying waste heat evaporator 13 communicates with the outlet of the deaerator in the waste heat recovery unit 10+11 and the heated effluent M2 of the process water waste heat heater 11, The inlet of the heated water M1 of the deaerator and process water waste heat heater 11 communicates with the condensed water outlet of the condenser 42 .

The waste heat recovery unit 10+11 includes the heat network return water waste heat heater 10, the inlet of the heat network return water inlet water M3 of the heat network return water waste heat heater 10 and the low temperature return water Rh of the hot water heater 46. The water pipes are connected, the outlet of the heat network return water inlet and outlet M4 of the heat network return water waste heat heater 10 is connected with the inlet of the low temperature return water Rh of the hot water heater 46, and the high temperature side inlet of the heat network return water waste heat heater 10 It is connected with the outlet of the sewage secondary steam L of the waste heat evaporation crystallizer 8, the outlet of the second drainage D2 on the high temperature side of the heat network return water waste heat heater 10 is connected with the first water discharge on the high temperature side of the deaerator and the process water waste heat heater 11 After the outlet of D1 is connected, it communicates with the inlet of the regenerated raw water D of the desalted water reverse osmosis membrane 23 .

The multi-media filter 1 of the thermal sewage treatment and resource utilization section A1 is also provided with an external concentrated water Pw inlet, which communicates with the water inlet pipeline of the low-concentration sewage source in the public sewage inflow outside the thermal power plant. The mixed water pretreatment tank 4 of the sewage treatment and resource utilization section A1 is also provided with an external high-concentration raw water Gw inlet, which communicates with the water inlet pipeline of the higher-concentration sewage source in the public sewage inflow outside the thermal power plant. The crystallized salt repurification device 9 of the sewage treatment and resource utilization section A1 is also provided with a feed port of the public external primary industrial salt Kw other than the thermal power plant.

It should be noted that this utility model proposes how to comprehensively solve the problem of recycling water resources and material resources of thermal power plants and other sewage by using heat exchange methods, waste heat evaporation and energy cascade utilization methods, and according to this overall solution can be There are different specific implementation measures and specific implementation devices with different structures, and the above specific implementation is only one of them. Any other similar simple deformation implementation, for example, involves the selection of the waste heat recovery heat exchanger type and The number of units changes; the type of waste heat heat source adopts low-pressure steam below 100°C, positive pressure steam above atmospheric pressure, or waste heat hot water, flue gas and other waste heat types; only a part of the claims are implemented but not all of them are driven by waste heat Evaporation method, or sewage pretreatment process, or post-treatment process, etc.; or combine the sewage pretreatment tank with the desulfurization sewage pretreatment tank, and other simple combination or separate design of the treatment equipment or process; or simply replace different types , performance and quality membranes or other sewage treatment devices for sewage treatment in the corresponding links; or other deformation methods that ordinary professionals can think of; or apply this technology to other countries with the same or similar methods, systems and structures Similar desulfurization water treatment and application occasions in the industry all fall into the protection scope of the present utility model.

Claims (8)

1. a kind of sewage zero-discharge and resource recovering system based on the driving of steam power plant's waste heat, total system includes four big boards Block, i.e. thermal method waste water control and recycling plate (A1), demineralized water plate (A2), boiler and recuperation of heat plate (A3), steam turbine Auxiliary line facility between power generation and waste heat recycling plate (A4) and plate interiors and plate, which is characterized in that steam turbine hair Electricity and the condenser (42) of waste heat recycling plate (A4) use low vacuum heat exchange structure, and boiler and recuperation of heat plate (A3), which remove, includes Further include flue gas contaminated water evaporator (37) outside boiler body (33) and its conventional auxiliary system and is carried based on inlet air of boiler vapor The residual heat from boiler fume of thermal cycle recycles component (30), the more medium filter of thermal method waste water control and recycling plate (A1) (1) outlet of the demineralized water concentrated water (P1) of the import and demineralized water plate (A2) of demineralized water concentrated water (P1) is connected, multimedium mistake The import of the cooling tower sewerage (P2) of filter (1) and steam turbine power generation and the cooling tower (44) of waste heat recycling plate (A4) it is cold But the outlet of tower sewerage (P2) is connected, the outlet of the high concentrated water of suspension (G9) of more medium filter (1) and flocculation sedimentation tank (21) original water inlet is connected, the filters pressing water out phase of the filters pressing water inlet and the first filter press (20) of more medium filter (1) Even, the processing water out of more medium filter (1) is connected with the original water inlet of first-stage reverse osmosis film (2), first-stage reverse osmosis film (2) Level-one clear water (D5) outlet and the import phase of the regeneration raw water (D) of the demineralized water reverse osmosis membrane (23) of demineralized water plate (A2) Even, the processing water out of first-stage reverse osmosis film (2) is connected with the original water inlet of two-pass reverse osmosis film (3), two-pass reverse osmosis film (3) The outlet of second level clear water (D4) be connected with the import of the regeneration raw water (D) of demineralized water reverse osmosis membrane (23), two-pass reverse osmosis film (3) processing water out is connected with the import of the highly concentrated raw water (G) of mixed water pretreatment pond (4), and the import of highly concentrated raw water (G) also divides Not in including coming from first-stage reverse osmosis film (2), two-pass reverse osmosis film (3), hyperfiltration/microfiltration film processing unit (6), the second filter press (15), it comes from the source water pretreatment pool (22) of demineralized water plate (A2), demineralized water reverse osmosis membrane (23), come from boiler and heat time Highly concentrated drain outlet including the desulfurizing tower (34) of receipts plate (A3) communicates, and mixes the high concentrated water of blowdown (G1) of water pretreatment pond (4) Outlet be connected with the original water inlet of the second filter press (15), mix water pretreatment pond (4) processing water out and oxidation calcification pond (5) original water inlet is connected, and oxidation calcification pond (5) is provided with the throwing of the import of oxidant (O), milk of lime and composite drug (F) Material mouth, the discharge port of calcium sulfate (K3), the discharge port of other solid salts (K5), processing water out, aoxidize the processing of calcification pond (5) Water out is connected with the original water inlet of hyperfiltration/microfiltration film processing unit (6), and hyperfiltration/microfiltration film processing unit (6) is provided with lye (CH) outlet of feed inlet, regenerated sewage (G3) and processing water out, the processing water of hyperfiltration/microfiltration film processing unit (6) go out Mouth divides the original water inlet of salt device (7) to be connected with nanofiltration membrane, and nanofiltration membrane divides the outlet and oxidation of the high concentrated water (H) of salt device (7) The import of the high concentrated water (H) in calcification pond (5) is connected, and nanofiltration membrane divides the treated water outlet and waste heat crystallizing evaporator of salt device (7) (8) original water inlet is connected, and the import for heat source (J1) that have surplus heat, waste heat heat source water outlet (J2) is arranged in waste heat crystallizing evaporator (8) Outlet, industrial grade sodium chloride (K1) salt outlet, sewage secondary steam (L) outlet and mother liquor (G4) outlet, wherein remaining The high temperature side-entrance phase of the outlet of the sewage secondary steam (L) of thermal evaporation crystallizer (8) and waste-heat recoverer component (10+11) Even, the high temperature side condensation water out and the regeneration raw water (D) of demineralized water reverse osmosis membrane (23) of waste-heat recoverer component (10+11) Import communicates, original water inlet phase of the processing water out of hyperfiltration/microfiltration film processing unit (6) also with negative pressure residual evaporator (14) Even, negative pressure residual evaporator (14) is provided with the import of the first low temperature exhaust heat heat source (R1), the water outlet of the first low temperature exhaust heat heat source (R2) import of outlet, the second low temperature exhaust heat heat source (R3), the outlet of the second low temperature exhaust heat heat source water outlet (R4), low pressure sewage The outlet of secondary steam (Ld) and the outlet of low pressure mother liquor (G5), the outlet of mesolow mother liquor (G5) and mother liquor desiccation waste heat steam The original water inlet for sending out device (13) is connected, and the import for heat source (J1) that have surplus heat, waste heat heat is arranged in mother liquor desiccation residual evaporator (13) Source is discharged the discharge port of the outlet of (J2), mother liquor desiccation solid waste (K6), and the low pressure sewage secondary of negative pressure residual evaporator (14) steams The outlet of vapour (Ld) is connected with the steam inlet of circulating cooling water- to-water heat exchanger (12), the cooling of circulating cooling water- to-water heat exchanger (12) into The import of water (N1) is connected with the cooling water outlet of cooling tower (44), the cooling water outlet (N2) of circulating cooling water- to-water heat exchanger (12) Outlet be connected with the cooling water inlet of cooling tower (44), the outlet of the low pressure clear water (D3) of circulating cooling water- to-water heat exchanger (12) with remove The import of the regeneration raw water (D) of salt water reverse osmosis membrane (23) communicates.

2. sewage zero-discharge and resource recovering system as described in claim 1 based on the driving of steam power plant's waste heat, feature exist In the waste heat crystallizing evaporator (8) industrial grade sodium chloride (K1) salt outlet and crystal salt again purification device (9) into Material mouth communicates, and the have surplus heat import of heat source (J1), the outlet of coagulation hydroenergy backwater (J2), height is arranged in purification device (9) to crystal salt again The discharge port of grade industrial grade sodium chloride (K4).

3. sewage zero-discharge and resource recovering system as described in claim 1 based on the driving of steam power plant's waste heat, feature exist In the import of the boiler and the high-temperature smoke discharging (Y) of the flue gas contaminated water evaporator (37) of recuperation of heat plate (A3) and from boiler Or the flue of the high-temperature smoke discharging (Y) of deduster is connected, the outlet and desulfurization of the medium temperature flue gas (Y0) of flue gas contaminated water evaporator (37) The import of the desulfurization of tower (34) into cigarette (Y1) is connected, import and waste heat of the spray of flue gas contaminated water evaporator (37) with mother liquor (G4) The outlet of the mother liquor (G4) of crystallizing evaporator (8) communicates or the outlet of the low pressure mother liquor (G5) of negative pressure residual evaporator (14) It communicates or the outlet in other high concentration stain diseases source communicates, it is solid that flue gas contaminated water evaporator (37) is additionally provided with flue gas desiccation The discharge port of useless (K7).

4. sewage zero-discharge and resource recovering system as described in claim 1 based on the driving of steam power plant's waste heat, feature exist It include residual heat from boiler fume compound spray tower (31) in residual heat from boiler fume recycling component (30), residual heat from boiler fume is multiple The gas inlet for closing spray column (31) is communicated with the outlet of the desulfurization fume (Y1) of desulfurizing tower (34), the compound spray of residual heat from boiler fume Drench the outlet of the fume afterheat high-temperature water (Rg1) of tower (31) and the first low temperature exhaust heat heat source (R1) of negative pressure residual evaporator (14) Import communicate, more than the import of the fume afterheat water at low temperature (Rh2) of residual heat from boiler fume compound spray tower (31) and the first low temperature The outlet of heat source water outlet (R2) communicates.

5. sewage zero-discharge and resource recovering system as described in claim 1 based on the driving of steam power plant's waste heat, feature exist In the steam turbine power generation and waste heat recycling plate (A4) condenser (42) recirculated water water outlet (Rg3) outlet in addition to The cooling water inlet of cooling tower (44) be connected it is outer, also with the second low temperature exhaust heat heat source (R3) of negative pressure residual evaporator (14) into Mouth communicates, and the import of the recirculated water water inlet (Rh4) of condenser (42) with the cooling water outlet of cooling tower (44) other than being connected, also It is communicated with the outlet of the second low temperature exhaust heat heat source water outlet (R4).

6. sewage zero-discharge and resource recovering system as described in claim 1 based on the driving of steam power plant's waste heat, feature exist In the steam turbine power generation and waste heat recycling plate (A4) steam turbine (43) steam extraction outlet in addition to feed-water heater group The high temperature side of the hot-water heater (46) of the air intake of part (40), the air intake of oxygen-eliminating device (41) and heating or technique heat user into Mouthful be connected outer, also communicated with the import of the waste heat heat source (J1) of waste heat crystallizing evaporator (8), or with crystal salt purification device again (9) import of waste heat heat source (J1) communicates, or the import with the waste heat heat source (J1) of mother liquor desiccation residual evaporator (13) It communicates, the condensation of the condensation water inlet of oxygen-eliminating device (41) in addition to condensation water out, hot-water heater (46) with condenser (42) The outlet of water return water (J2) communicate it is outer, also and from waste heat crystallizing evaporator (8) or crystal salt purification device (9), mother liquor again The outlet of the coagulation hydroenergy backwater (J2) of desiccation residual evaporator (13) communicates, also with removing in waste-heat recoverer component (10+11) The outlet for being heated water outlet (M2) of oxygen device and process water heater heated by waste heat (11) communicates, oxygen-eliminating device and process water heater heated by waste heat (11) the import being heated into water (M1) is communicated with the condensation water out of condenser (42).

7. sewage zero-discharge and resource recovering system as described in claim 1 based on the driving of steam power plant's waste heat, feature exist In the waste-heat recoverer component (10+11) include heat supply network return water heater heated by waste heat (10), heat supply network return water heater heated by waste heat (10) import of heat supply network return water water inlet water (M3) is communicated with the water pipe that comes of the low-temperature return water (Rh) of hot-water heater (46), heat The outlet of water (M4) and the low-temperature return water of hot-water heater (46) are gone in the heat supply network return water water inlet of net return water heater heated by waste heat (10) (Rh) import communicates, the high temperature side-entrance of heat supply network return water heater heated by waste heat (10) and the sewage two of waste heat crystallizing evaporator (8) The outlet of secondary steam (L) is connected, and the high temperature side second of heat supply network return water heater heated by waste heat (10) drains outlet and the oxygen-eliminating device of (D2) And after the outlet of the draining of high temperature side first (D1) of process water heater heated by waste heat (11) is connected, with demineralized water reverse osmosis membrane (23) The import of regeneration raw water (D) communicates.

8. sewage zero-discharge and resource recovering system as described in claim 1 based on the driving of steam power plant's waste heat, feature exist In the more medium filter (1) of the thermal method waste water control and recycling plate (A1) be additionally provided with external concentrated water (Pw) into Mouthful, it is communicated with the inlet pipeline of the low concentration sewage source in the public wastewater influent except steam power plant, thermal method sewage is controlled The mixed water pretreatment pond (4) of reason and recycling plate (A1) is additionally provided with the import of external highly concentrated raw water (Gw), with steam power plant Except public wastewater influent in the inlet pipeline of higher concentration sewage source communicate, thermal method waste water control and recycling plate (A1) purification device (9) is additionally provided with the charging of the public external primary industry salt (Kw) except steam power plant to crystal salt again Mouthful.