CN109179538B - Desulfurization waste water concentration, evaporation and crystallization integrated zero emission treatment system - Google Patents
Desulfurization waste water concentration, evaporation and crystallization integrated zero emission treatment system Download PDFInfo
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- CN109179538B CN109179538B CN201811138967.0A CN201811138967A CN109179538B CN 109179538 B CN109179538 B CN 109179538B CN 201811138967 A CN201811138967 A CN 201811138967A CN 109179538 B CN109179538 B CN 109179538B
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 61
- 230000023556 desulfurization Effects 0.000 title claims abstract description 59
- 239000002351 wastewater Substances 0.000 title claims abstract description 48
- 238000001704 evaporation Methods 0.000 title claims abstract description 44
- 230000008020 evaporation Effects 0.000 title claims abstract description 41
- 238000002425 crystallisation Methods 0.000 title claims abstract description 13
- 230000008025 crystallization Effects 0.000 title claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000010438 heat treatment Methods 0.000 claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000003860 storage Methods 0.000 claims abstract description 12
- 230000003009 desulfurizing effect Effects 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 11
- 238000012544 monitoring process Methods 0.000 claims description 4
- -1 polytetrafluoroethylene Polymers 0.000 claims description 4
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 4
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 3
- 210000002445 nipple Anatomy 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 19
- 230000008569 process Effects 0.000 abstract description 18
- 238000012423 maintenance Methods 0.000 abstract description 6
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 239000002002 slurry Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 238000012806 monitoring device Methods 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Abstract
A desulfurization wastewater concentration, evaporation and crystallization integrated zero emission treatment system comprises a concentration evaporator, a vapor compressor, a vapor storage device, an evaporation heat exchange surface, a vapor condensate storage device, a water-vapor separation box and a natural circulation heating device which are sequentially and circularly communicated. The evaporation heat exchange surface is positioned in the concentration evaporator, the upper end of the evaporation heat exchange surface extends out of the concentration evaporator and is communicated with the steam storage device positioned on the top surface of the concentration evaporator, and the lower end of the evaporation heat exchange surface is communicated with the steam condensate storage device positioned in the concentration evaporator. The lower part of the concentrating evaporator is a desulfurization wastewater part, and the upper part of the concentrating evaporator is a low-temperature steam part; the low-temperature steam of the low-temperature steam part is pumped into the steam compressor through the first pipeline, and is pressurized and heated in the steam compressor to form high-pressure high-temperature steam, and the temperature difference between the low-temperature steam and the high-pressure high-temperature steam is 8-10 ℃. The invention solves the problems of long flow, complex flow, high investment and high operation and maintenance cost of the existing desulfurization wastewater treatment process.
Description
Technical Field
The invention relates to the field of desulfurization wastewater treatment, in particular to a zero-emission treatment system integrating concentration, evaporation and crystallization of desulfurization wastewater.
Background
The wet desulfurization of flue gas limestone-gypsum in coal-fired boiler is the most widely used sulfur dioxide removal process in China at present. The outstanding advantages are as follows: high desulfurization efficiency, recoverable gypsum, mature and reliable process and strong adaptability to the change of sulfur content of coal and boiler load. In the circulating absorption slurry of the wet desulfurization tower, chlorine ion CL-injection is enriched: mainly from HCl in flue gas, and high concentration CL-has strong corrosiveness to metals, so that the chloride ion concentration in the circulating slurry is generally required to be controlled within 20000 ppm. The chloride ion concentration in the circulating slurry can be reduced by discharging a certain volume of circulating slurry, and the chloride ion concentration is lower as more circulating slurry is discharged. In actual engineering, a single 300MW unit is subjected to wet desulfurization, and 3-4 m < 3 >/h is generally required to be discharged; the emission of a single 600MW unit is required to be 5-6 m < 3 >/h. This is the source of desulfurization waste water.
The desulfurization waste water can not be directly discharged, and needs to be subjected to pH value adjustment, organic sulfur addition to remove heavy metals, coagulation/coagulant aid addition and sodium hypochlorite addition to remove COD, and finally enters a clarifier/concentrator. The supernatant liquid of the clarifier/concentrator meets the primary or secondary wastewater comprehensive discharge standard GB8978-1996 for discharge; the sludge deposited on the lower part is dehydrated to form a mud cake, and the mud is delivered to units conforming to relevant qualification for disposal.
In recent years, with the improvement of environmental protection consciousness and the increasingly stringent environmental protection regulations, energy conservation and environmental protection are widely paid attention to. The desulfurization wastewater is treated by the conventional process, and can reach the comprehensive sewage discharge standard, but the desulfurization wastewater is polluted on the receiving water body after all. Therefore, at present, more and more power plants in China are required to carry out zero emission treatment on desulfurization wastewater. On the basis of the conventional treatment process as pretreatment, the treated fresh water is recycled through ultrafiltration and reverse osmosis treatment, and the reduced concentrated water is evaporated to dryness through an evaporation device, so that zero emission of desulfurization wastewater is realized.
The typical output process flow of the desulfurization wastewater zero emission is long and complex, and the investment and the operation and maintenance cost are high, so that the development of a process treatment system with shorter process flow and lower investment and operation and maintenance cost is urgent.
Disclosure of Invention
The invention aims to provide a zero-emission treatment system integrating concentration, evaporation and crystallization of desulfurization wastewater, which aims to solve the problems of long flow, complex flow, high investment and high operation and maintenance cost of the existing desulfurization wastewater treatment process.
In order to achieve the above purpose, the invention adopts the following technical scheme:
a desulfurization wastewater concentration, evaporation and crystallization integrated zero emission treatment system comprises a concentration evaporator, a vapor compressor, a vapor storage device, an evaporation heat exchange surface, a vapor condensate storage device, a water-vapor separation box and a natural circulation heating device which are sequentially and circularly communicated.
The evaporation heat exchange surface is positioned in the concentration evaporator, the upper end of the evaporation heat exchange surface extends out of the concentration evaporator and is communicated with the steam storage device positioned on the top surface of the concentration evaporator, and the lower end of the evaporation heat exchange surface is communicated with the steam condensate storage device positioned in the concentration evaporator.
The lower part of the concentrating evaporator is a desulfurization wastewater part, and the upper part of the concentrating evaporator is a low-temperature steam part; the low-temperature steam of the low-temperature steam part is pumped into the steam compressor through the first pipeline, and is pressurized and heated in the steam compressor to form high-pressure high-temperature steam, and the temperature difference between the low-temperature steam and the high-pressure high-temperature steam is 8-10 ℃.
The evaporation heat exchange surface comprises a group of heat exchange tube bundles which are vertically arranged.
One end of the heat exchange tube bundle is restrained in the steam container, the other end of the heat exchange tube bundle is restrained in the steam condensate container, and the middle part of the heat exchange tube bundle is in a semi-free swinging state in desulfurization wastewater of the desulfurization wastewater part at the lower part of the concentration evaporator.
The heat exchange tube bundle is a polytetrafluoroethylene tube with the diameter of 10mm and the wall thickness of 1 mm.
The upper part of the water-steam separation tank is a steam part, and the lower part of the water-steam separation tank is a condensed water part; the inlet of the evaporator is positioned at one side of the steam part and is communicated with the steam condensate receiver through a second pipeline, the steam outlet is positioned at the top end of the steam part and is communicated with the top surface of the concentration evaporator through a third pipeline, the circulating condensate outlet is positioned at the bottom end of the condensate part and is communicated with the natural circulation heating device through a fourth pipeline, and the externally discharged condensate outlet is positioned at one side of the condensate part and is externally discharged through a fifth pipeline.
The natural circulation heating device is positioned in the inlet flue of the desulfurizing tower.
The natural circulation heating device comprises a group of heating tube bundles which are vertically arranged, the top ends of the heating tube bundles are higher than the upper opening of the inlet flue of the desulfurizing tower, and the bottom ends of the heating tube bundles exceed the lower opening of the inlet flue of the desulfurizing tower.
The lower port of the heating tube bundle is communicated with the water outlet of the fourth pipeline, and the upper port of the heating tube bundle is communicated with the other side of the condensate water part of the water-vapor separation tank through the sixth pipeline.
The concentrating evaporator comprises an upper part and a lower part, wherein the upper part of the concentrating evaporator is a cylindrical part in a cylindrical shape, the lower part of the concentrating evaporator is a conical part in a conical shape, and the lower opening of the cylindrical part is in fit connection with the upper opening of the conical part.
The side wall of the column casing part of the concentration evaporator is sequentially provided with a first measuring connecting pipe, a second measuring connecting pipe and a third measuring connecting pipe which are used for installing a pressure sensor from top to bottom.
The first measuring connection pipe is flush with the top of the heat exchange tube bundle.
The third measuring connection pipe is flush with the bottom of the heat exchange tube bundle.
The second measuring adapter is arranged at the upper position of the Ji Huanre tube bundle.
And a solution density monitoring device is arranged in the concentration evaporator.
A seventh pipeline is arranged at the bottom of the concentration evaporator; the outer port of the seventh pipeline is communicated with the outside and is positioned at the bottom of the cylindrical part, and the inner port of the seventh pipeline extends to the bottom of the conical part.
The outer port of the seventh pipeline is respectively communicated with a desulfurization system water inlet pipeline and a concentrated product discharge pipeline through three-way connectors.
Compared with the prior art, the invention has the following characteristics and beneficial effects:
1. in the invention, the desulfurization wastewater is pretreated, concentrated, evaporated and crystallized into a whole; the heat source required by evaporation is mainly self-produced; adopting flue gas waste heat of an inlet flue of a desulfurizing tower as a supplementary heat source; the final product is concentrated crystalline solid and pure water of steam condensate water, and can be recycled, thus realizing zero emission of desulfurization wastewater; in addition, almost no water treatment agent is added in the process of treating the desulfurization wastewater by using the treatment system; the whole treatment system has short process flow, low investment and operation cost and energy conservation and emission reduction, and provides an economic and reasonable integrated concentration, evaporation and crystallization treatment system for desulfurization wastewater of a thermal power plant.
2. The traditional treatment system comprises a pretreatment device, an ultrafiltration device, a reverse osmosis device and an evaporation device, the number of the devices is large, the process flow is long and complex, and the maintenance is difficult.
The invention is provided with the concentrating evaporator, the concentration, evaporation and crystallization of the desulfurization wastewater can be completely finished in the concentrating evaporator, the quantity of the device is small, the process flow is shortened, and the investment and the operation and maintenance cost are reduced.
3. An evaporation heat exchange surface is arranged in the concentration evaporator, so that heat exchange between the desulfurization wastewater and self-produced high-temperature steam is realized; the medium in the heat exchange tube bundle of the evaporation heat exchange surface is high-pressure high-temperature steam, and the high-pressure high-temperature steam is contacted with the desulfurization wastewater in the concentrating evaporator outside the heat exchange tube bundle to realize boiling evaporation of the desulfurization wastewater in the concentrating evaporator, the desulfurization wastewater is continuously concentrated, evaporated and crystallized at the upper part of the concentrating evaporator, and the final solid is settled to the lower part of the concentrating evaporator and discharged under the action of gravity mainly NaCl and CaSO 4.
4. The evaporation heat exchange surface is made of small-aperture, thin-wall and polytetrafluoroethylene materials, has smooth surface and is not sticky, and can not be scaled and blocked; meanwhile, the heat exchange tube bundles are restrained at two ends only, the middle section is in a semi-free swinging state in the desulfurization wastewater, and the surface energy is self-cleaning; the two sides of the evaporation heat exchange surface realize phase change condensation or boiling heat exchange, and the heat exchange coefficient is large, so that the heat exchange area can be reduced, and the investment of equipment capital is reduced.
5. The method comprises the steps that a steam compressor is arranged, low-temperature steam evaporated from desulfurization wastewater is extracted from the upper part of a concentration evaporator by the steam compressor, the low-temperature steam is pressurized by the steam compressor and is heated to 8-10 ℃ and then becomes self-produced high-temperature steam, the self-produced high-temperature steam enters a heat exchange tube bundle, so that the temperature difference required by heat exchange is generated, a heat source evaporated from the desulfurization wastewater is taken from the self-produced high-temperature steam after evaporation and pressurization, and the self-production of the steam is realized; meanwhile, due to the suction effect of the vapor compressor, micro negative pressure is formed in the concentrating evaporator, so that the evaporating tower is normal-pressure equipment, and the operation is more stable and the safety is higher.
6. Waste heat of an inlet flue of the desulfurizing tower is used as an external supplementary heat source and is used as a starting heat source; the heat dissipation exists between the concentrating evaporator and the pipeline, and the temperature of the wastewater entering the concentrating evaporator is only about 50 ℃ and needs to be heated to the boiling point, so that the whole process cannot achieve self-supply of 100% of heat sources; the natural circulation heating device is arranged in the flue gas temperature of the inlet flue of the desulfurizing tower above 110 ℃, the generated steam is used as a supplementary heat source, and the heated water in the natural circulation heating device adopts condensed water generated by the concentration evaporator.
The invention can be widely applied to wastewater treatment systems.
Drawings
The invention is described in further detail below with reference to the accompanying drawings.
FIG. 1 is a schematic process flow diagram of the integrated desulfurization wastewater concentration, evaporation and crystallization zero-emission treatment system of the present invention.
Reference numerals: 1-concentrating evaporator, 2-vapor compressor, 3-vapor separation box/liquid level control box, 4-natural circulation heating device, 5-evaporating heat exchange surface, 6-vapor container, 7-vapor condensate container, 8-first pipeline, 9-second pipeline, 10-third pipeline, 11-fourth pipeline, 12-fifth pipeline, 13-sixth pipeline, 14-seventh pipeline, 15-first measuring connecting pipe, 16-second measuring connecting pipe, 17-third measuring connecting pipe, 18-desulfurization system water inlet pipeline, 19-concentrated product discharge pipeline and 20-desulfurization tower inlet flue.
Detailed Description
Referring to fig. 1, the embodiment shows a desulfurization wastewater concentration, evaporation and crystallization integrated zero emission treatment system, which comprises a concentration evaporator 1, a vapor compressor 2, a vapor receiver 6, an evaporation heat exchange surface 5, a vapor condensate receiver 7, a water-vapor separation tank 3 and a natural circulation heating device 4 which are sequentially and circularly communicated; the evaporation heat exchange surface 5 is positioned in the concentration evaporator 1, the upper end of the evaporation heat exchange surface extends out of the concentration evaporator 1 and is communicated with the steam storage 6 positioned on the top surface of the concentration evaporator 1, and the lower end of the evaporation heat exchange surface is communicated with the steam condensate storage 7 positioned in the concentration evaporator 1; the lower part of the concentration evaporator 1 is a desulfurization waste water part, and the upper part is a low-temperature steam part; the low-temperature steam of the low-temperature steam part is pumped into the steam compressor 2 through the first pipeline 8, and is pressurized and heated in the steam compressor to form high-pressure high-temperature steam, and the temperature difference between the low-temperature steam and the high-pressure high-temperature steam is 8-10 ℃; the evaporation heat exchange surface 5 comprises a group of heat exchange tube bundles which are vertically arranged;
one end of the heat exchange tube bundle is restrained in the steam container 6, the other end of the heat exchange tube bundle is restrained in the steam condensate container 7, and the middle part of the heat exchange tube bundle is in a semi-free swinging state in desulfurization wastewater of the desulfurization wastewater part at the lower part of the concentration evaporator 1; the heat exchange tube bundle is a polytetrafluoroethylene tube with the diameter of 10mm and the wall thickness of 1 mm.
The upper part of the water-steam separation tank 3 is a steam part, and the lower part of the water-steam separation tank is a condensed water part; the inlet of the circulating condensate water heating device is positioned at one side of the steam part and is communicated with the steam condensate water container 7 through a second pipeline 9, the steam outlet is positioned at the top end of the steam part and is communicated with the top surface of the concentration evaporator 1 through a third pipeline 10, the circulating condensate water outlet is positioned at the bottom end of the condensate water part and is communicated with the natural circulation heating device 4 through a fourth pipeline 11, and the discharged condensate water outlet is positioned at one side of the condensate water part and is discharged and utilized through a fifth pipeline 12.
The natural circulation heating device 4 is positioned in the desulfurizing tower inlet flue 20; the natural circulation heating device 4 comprises a group of heating tube bundles which are vertically arranged, the top ends of the heating tube bundles are higher than the upper opening of the inlet flue 20 of the desulfurizing tower, and the bottom ends of the heating tube bundles are higher than the lower opening of the inlet flue 20 of the desulfurizing tower; the lower port of the heating tube bundle is communicated with the water outlet of the fourth pipeline 11, and the upper port of the heating tube bundle is communicated with the other side of the condensed water part of the water-vapor separation tank 3 through a sixth pipeline 13; a water vapor mixture in a sixth pipeline 13; the condensed water in the fourth pipe 11 naturally circulates down.
The concentrating evaporator 1 comprises an upper part and a lower part, wherein the upper part of the concentrating evaporator is a cylindrical part in a cylindrical shape, the lower part of the concentrating evaporator is a conical part in a conical shape, and the lower opening of the cylindrical part is in fit connection with the upper opening of the conical part; the parameters to be controlled by the processing system are as follows: concentrating the liquid level and the solution density in the evaporator; the processing system does not need too much parameter control, and is simple and easy to implement; a first measuring connecting pipe 15, a second measuring connecting pipe 16 and a third measuring connecting pipe 17 for installing a pressure sensor are sequentially arranged on one side wall of the cylindrical part of the concentration evaporator 1 from top to bottom, so that monitoring data of liquid level, density and the like are provided; the concentration evaporator is required to maintain the liquid level to be basically constant, the water inflow is controlled according to the actual liquid level monitoring data through the second measuring connecting pipe, and meanwhile, the water inflow is protected through the first measuring connecting pipe; the first measuring connection pipe 15 is flush with the top of the heat exchange tube bundle; the third measuring connection pipe 17 is flush with the bottom of the heat exchange tube bundle; the second measuring adapter 16 is arranged at the upper part of the Ji Huanre tube bundle; the concentration evaporator 1 is internally provided with a solution density monitoring device, the solution density in the concentration evaporator is controlled by the solution density monitoring device, and the discharge of solid matters is started according to the solution density; a seventh pipeline 14 is arranged at the bottom of the concentration evaporator 1; the outer port of the seventh pipeline 14 is communicated with the outside and is positioned at the bottom of the cylindrical part, and the inner port extends to the bottom of the conical part; the outer port of the seventh pipeline 14 is respectively communicated with a desulfurization system water inlet pipeline 18 and a concentrated product discharge pipeline 19 through a three-way joint; a first switch valve is arranged on the desulfurization system water inlet pipeline 18; a second switch valve is provided on the concentrated product discharge line 19.
The steam compressor is mechanical rotation equipment and is the most important energy consumption user in the treatment system, and the treatment system has lower requirements on steam pressurization and temperature rise, so that the domestic centrifugal steam compressor and the Roots type steam compressor can meet the requirements, and expensive imported equipment is not needed.
The process flow of the invention comprises the following steps: the temperature of desulfurization wastewater from the desulfurization system is about 50 ℃, the desulfurization wastewater enters the bottom of a concentration evaporator through a water inlet pipeline of the desulfurization system, and low-temperature steam on the upper part of the concentration evaporator is extracted by a steam compressor and is boosted and heated to rise in temperature: forming high-pressure high-temperature steam at 8-10 ℃, enabling the high-pressure high-temperature steam to enter a heating tube bundle of an evaporation heat exchange surface, performing heat exchange with desulfurization wastewater in a concentration evaporator, and realizing boiling evaporation of the desulfurization wastewater under a micro negative pressure condition, so that the desulfurization wastewater is continuously concentrated at the upper part of the concentration evaporator until the final solid matters of crystallization are mainly NaCl and CaSO 4; in the concentrating evaporator, the upper part of the concentrated desulfurization wastewater has larger specific gravity, the liquid in the concentrating evaporator can form natural convection, and finally solid particles enter the bottom of the concentrating evaporator and are discharged through a concentrated product discharge pipeline; the subsequent process can adopt centrifugal dehydration or plate-frame filter pressing process to further treat the discharged product.
The high-pressure high-temperature steam in the heating tube bundle is condensed after heat exchange with the desulfurization wastewater, flows downwards and is collected into the steam condensate receiver, is discharged into the water-steam separation tank through the fourth pipeline, and most of the steam condensate discharged into the water-steam separation tank is discharged and utilized through the fifth pipeline, a small amount of steam condensate is used as a supplementary water source of the natural circulation heating device in the inlet flue of the desulfurizing tower, generated steam is used as a supplementary heat source of the concentrating evaporator, and the heat of the supplementary heat source is only about 20% of the total heat requirement of the concentrating evaporator, so that the heat exchange area of the natural circulation heating device is smaller.
Claims (2)
1. A desulfurization waste water concentration, evaporation and integrative zero release processing system of crystallization, its characterized in that: comprises a concentrating evaporator (1), a vapor compressor (2), a vapor container (6), an evaporating heat-exchanging surface (5), a vapor condensate container (7), a vapor separation tank (3) and a natural circulation heating device (4) which are sequentially and circularly communicated;
the evaporation heat exchange surface (5) is positioned in the concentration evaporator (1), the upper end of the evaporation heat exchange surface extends out of the concentration evaporator (1) and is communicated with the steam storage device (6) positioned on the top surface of the concentration evaporator (1), and the lower end of the evaporation heat exchange surface is communicated with the steam condensate storage device (7) positioned in the concentration evaporator (1);
the lower part of the concentrating evaporator (1) is a desulfurization wastewater part, and the upper part is a low-temperature steam part; the low-temperature steam of the low-temperature steam part is pumped into a steam compressor (2) through a first pipeline (8), and is pressurized and heated in the steam compressor to form high-pressure high-temperature steam, and the temperature difference between the low-temperature steam and the high-pressure high-temperature steam is 8-10 ℃;
the evaporation heat exchange surface (5) comprises a group of heat exchange tube bundles which are vertically arranged;
one end of the heat exchange tube bundle is restrained in the steam container (6), the other end of the heat exchange tube bundle is restrained in the steam condensate container (7), and the middle part of the heat exchange tube bundle is in a semi-free swinging state in desulfurization wastewater of the desulfurization wastewater part at the lower part of the concentration evaporator (1);
the heat exchange tube bundle is a polytetrafluoroethylene tube with the diameter of 10mm and the wall thickness of 1 mm;
the upper part of the water-steam separation tank (3) is a steam part, and the lower part of the water-steam separation tank is a condensed water part; the inlet of the evaporator is positioned at one side of the steam part and is communicated with the steam condensate receiver (7) through a second pipeline (9), the steam outlet is positioned at the top end of the steam part and is communicated with the top surface of the concentration evaporator (1) through a third pipeline (10), the circulating condensate outlet is positioned at the bottom end of the condensate part and is communicated with the natural circulation heating device (4) through a fourth pipeline (11), and the discharged condensate outlet is positioned at one side of the condensate part and is discharged and utilized through a fifth pipeline (12);
the natural circulation heating device (4) is positioned in an inlet flue (20) of the desulfurizing tower;
the natural circulation heating device (4) comprises a group of heating tube bundles which are vertically arranged, the top ends of the heating tube bundles are higher than the upper opening of the inlet flue (20) of the desulfurizing tower, and the bottom ends of the heating tube bundles are higher than the lower opening of the inlet flue (20) of the desulfurizing tower;
the lower port of the heating tube bundle is communicated with the water outlet of the fourth pipeline (11), and the upper port of the heating tube bundle is communicated with the other side of the condensed water part of the water-vapor separation tank (3) through a sixth pipeline (13);
the concentrating evaporator (1) comprises an upper part and a lower part, wherein the upper part of the concentrating evaporator is a cylindrical part in a cylindrical shape, the lower part of the concentrating evaporator is a conical part in a conical shape, and the lower opening of the cylindrical part is in fit connection with the upper opening of the conical part;
a first measuring connecting pipe (15), a second measuring connecting pipe (16) and a third measuring connecting pipe (17) for installing a pressure sensor are sequentially arranged on the side wall of the column casing part of the concentration evaporator (1) from top to bottom; thereby providing liquid level and density monitoring data; the concentration evaporator is required to maintain the liquid level constant, the water inflow is controlled according to the actual liquid level monitoring data through the second measuring connecting pipe, and meanwhile, the water inflow is protected through the first measuring connecting pipe;
the first measuring connection pipe (15) is level with the set highest control liquid level;
the third measuring connecting pipe (17) is level with the bottom of the heat exchange tube bundle;
the second measuring nipple (16) is located in the middle-upper position of the Ji Huanre tube bundle.
2. The desulfurization wastewater concentration, evaporation and crystallization integrated zero-emission treatment system according to claim 1, wherein: a seventh pipeline (14) is arranged at the bottom of the concentration evaporator (1); the outer port of the seventh pipeline (14) is communicated with the outside and is positioned at the bottom of the cylindrical part, and the inner port of the seventh pipeline extends to the bottom of the conical part;
the outer port of the seventh pipeline (14) is respectively communicated with a desulfurization system water inlet pipeline (18) and a concentrated product discharge pipeline (19) through three-way connectors.
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