CN114195212A - Novel desulfurization wastewater evaporative crystallization process and equipment - Google Patents
Novel desulfurization wastewater evaporative crystallization process and equipment Download PDFInfo
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- CN114195212A CN114195212A CN202111215705.1A CN202111215705A CN114195212A CN 114195212 A CN114195212 A CN 114195212A CN 202111215705 A CN202111215705 A CN 202111215705A CN 114195212 A CN114195212 A CN 114195212A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 98
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 74
- 230000023556 desulfurization Effects 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000002425 crystallisation Methods 0.000 title claims abstract description 29
- 230000008025 crystallization Effects 0.000 title claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000003507 refrigerant Substances 0.000 claims abstract description 47
- 239000002918 waste heat Substances 0.000 claims abstract description 30
- 238000001704 evaporation Methods 0.000 claims abstract description 28
- 230000008020 evaporation Effects 0.000 claims abstract description 26
- 238000001816 cooling Methods 0.000 claims abstract description 7
- 238000009833 condensation Methods 0.000 claims abstract description 5
- 230000005494 condensation Effects 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims description 39
- 239000007789 gas Substances 0.000 claims description 17
- 239000012071 phase Substances 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 8
- 239000013589 supplement Substances 0.000 claims description 5
- 229910000619 316 stainless steel Inorganic materials 0.000 claims description 3
- 229910000589 SAE 304 stainless steel Inorganic materials 0.000 claims description 3
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 25
- 230000006835 compression Effects 0.000 abstract description 4
- 238000007906 compression Methods 0.000 abstract description 4
- 238000010438 heat treatment Methods 0.000 abstract 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910001424 calcium ion Inorganic materials 0.000 description 4
- 229910001425 magnesium ion Inorganic materials 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 230000001502 supplementing effect Effects 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
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- 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
- 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
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a novel desulfurization wastewater evaporative crystallization process and equipment, which utilize the working principle of a compression heat pump to recover sensible heat and latent heat released in the secondary steam cooling and condensing process and sensible heat released in the low-pressure steam condensate cooling process to heat desulfurization wastewater entering a system, thereby greatly saving the heat consumed in the evaporative concentration process. The refrigerant forms a closed cycle in the system; the desulfurization wastewater enters a separator firstly, then is sent into a heater for heating through a forced circulation pump, and then enters the separator for evaporation; the generated secondary steam firstly enters a condenser for cooling and condensation and then enters a condensate water tank; the concentrated desulfurization wastewater is sent into the heater again through a forced circulation pump to realize forced circulation evaporation, and is sent to a downstream device through a concentrated water pipeline after reaching the target concentration ratio. The invention adopts the low-temperature heat pump evaporation technology to carry out concentration and decrement on the desulfurization wastewater, recovers the waste heat of secondary steam and steam condensate to the maximum extent, and improves the energy utilization efficiency.
Description
Technical Field
The invention relates to the technical field of wet desulphurization, in particular to a novel desulphurization wastewater evaporative crystallization process and equipment.
Background
The wet desulphurization process has the advantages of high desulphurization efficiency, low operation cost, mature technology, simple operation and the like, and occupies an absolutely dominant position in the field of flue gas desulphurization purification treatment. The wet desulphurization technology accounts for more than 95% in the domestic flue gas desulphurization purification field and more than 99% in the flue gas ultra-low emission treatment field.
A certain amount of waste water is generated in the wet desulphurization process, and the waste water is used as terminal waste water of a power plant, so that the water quality is the worst. The salt-free high-concentration calcium carbonate contains heavy metals, a large amount of calcium, magnesium, chloride ions and the like, and has the characteristics of high salt content, high suspended matter content, high COD (chemical oxygen demand) and the like. The existence of calcium and magnesium ions can cause the scaling problem of a subsequent treatment unit, and the existence of a large amount of chloride ions can cause flue corrosion to further influence the safe operation of equipment.
The conventional desulfurization wastewater zero-discharge technology mainly comprises the following steps: a pretreatment technology of the desulfurization wastewater, a concentration and decrement technology and an evaporation and crystallization technology. Most of the main process routes are the permutation and combination of the three technologies.
The desulfurization wastewater has high content of suspended substances, calcium ions and magnesium ions, especially calcium sulfate in a supersaturated state, has high scaling tendency, and needs to be pretreated and added with a medicament for softening in order to ensure the stable operation of a subsequent process. The dosage of the medicament is large, the dosing cost is high, and a large amount of sludge can be generated, so that new pollution is brought to the environment;
the concentration and decrement aims to reduce the water quantity of the desulfurization wastewater and reduce the treatment pressure of an evaporative crystallization system. The concentration and decrement technology is divided into membrane concentration and thermal concentration. The high-rate concentration of the desulfurization wastewater can be realized by adopting the membrane method for concentration, but the problems of high investment, cleaning and maintenance cost, easy pollution and blockage and the like exist, and the wastewater needs to be subjected to deep pretreatment to meet the water inlet requirement of a membrane system; the thermal method is adopted for concentration, the requirement on water quality is low, the concentration can be directly carried out without pretreatment by effectively controlling the concentration ratio, but low-pressure steam is adopted, the application range is limited, and the cost is high.
The evaporative crystallization technology is divided into bypass flue evaporation, MVR evaporative concentration and multi-effect evaporative crystallization, wherein the bypass flue evaporation is the mainstream technology at present due to the advantages of small investment, low operation cost, low water consumption and low energy consumption.
Disclosure of Invention
The invention aims to solve the technical problem of providing a novel desulfurization wastewater evaporative crystallization process and equipment, which utilize the working principle of a compression heat pump to recover sensible heat and latent heat released in the secondary steam cooling and condensation process and sensible heat released in the low-pressure steam condensate cooling process to heat desulfurization wastewater entering a system, thereby greatly saving the heat consumed in the evaporative concentration process, realizing the concentration and decrement of the desulfurization wastewater under high concentration multiple, adopting the low-temperature heat pump evaporation technology to recover the waste heat of the secondary steam and the steam condensate to the maximum extent and improving the energy utilization efficiency.
In order to solve the above technical problem, an embodiment of the present invention provides the following technical solutions:
a novel desulfurization wastewater evaporative crystallization process comprises the following steps:
1) desulfurization wastewater enters a separator through a wastewater feeding pump, is sent into a heater through a forced circulation pump to be heated to absorb heat, and then enters the separator to be evaporated; feeding the concentrated desulfurization wastewater in the separator into a heater again through a forced circulation pump;
2) the secondary steam generated by the evaporation of the desulfurization wastewater in the separator exchanges heat with the liquid dividing wall of the refrigerant in the condenser, so that the temperature is reduced and the secondary steam is condensed to form secondary steam condensate which enters the condensate tank;
3) the refrigerant forms closed circulation among condenser, steam condensate waste heat recoverer, vapour and liquid separator, compressor, heater, reservoir, filter, choke valve:
wherein, the liquid refrigerant is evaporated in the condenser to absorb a large amount of heat, so that the secondary steam is cooled and condensed, and the refrigerant steam is condensed in the heater to release a large amount of heat, so that the desulfurization wastewater is heated;
the gas refrigerant enters the compressor after passing through the gas-liquid separator, the pressure and the temperature are increased after compression, then the gas refrigerant enters the heater to release heat and condense into liquid, the desulfurization wastewater in the heater is heated, the liquid refrigerant returns to the condenser after passing through the liquid accumulator, the filter and the throttle valve, and the heat is absorbed and vaporized in the condenser, so that the refrigerant circulation is completed.
Preferably, the desulfurization wastewater in the step 1) exchanges heat with a refrigerant steam partition wall in a heater to realize temperature rise, and the temperature rise enters a separator to be evaporated.
Preferably, after the secondary steam condensate water in the step 2) enters a condensate water tank, the non-condensable gas and the condensate water are respectively pumped out through a vacuum pump and a condensate water pump.
Preferably, the heater adopts a multi-channel heat exchanger, the part of the desulfurization wastewater, which is insufficient in heat required by evaporative crystallization, is supplemented by low-pressure steam, and different target concentration ratios of the desulfurization wastewater are adjusted by adjusting the using amount of the low-pressure steam.
The invention also provides novel desulfurization wastewater evaporative crystallization equipment, which comprises a wastewater feeding pump, a separator, a forced circulation pump, a heater, a condenser, a condensed water tank, a gas-liquid separator, a compressor, a liquid storage device, a filter, a throttle valve and a steam condensed water waste heat recoverer, wherein the output end of the wastewater feeding pump is connected with the first wastewater input end of the separator;
the steam condensate waste heat recovery device is characterized in that a refrigerant gas phase output end of the condenser is connected with the steam condensate waste heat recovery device, the gas-liquid separator and the compressor are sequentially connected, an output end of the compressor is connected with a refrigerant gas phase input end of the heater, and a refrigerant liquid phase output end of the heater is connected with a refrigerant liquid phase input end of the condenser sequentially through the liquid storage device, the filter and the throttle valve.
Preferably, the heater is further connected with a steam condensate water waste heat recoverer.
Preferably, the heater is further provided with a low-pressure steam supplementing end, and the low-pressure steam supplementing end is connected with the output end of the low-pressure steam equipment.
Preferably, the output end of the condensed water tank is connected with a vacuum pump and a condensed water pump.
Preferably, the heater adopts a tube type heat exchanger, and the heat exchange tube of the heater is made of 2205 and 2507 steel.
Preferably, the condenser adopts a tube type heat exchanger, the steam condensate waste heat recoverer adopts a plate type heat exchanger, and the heat exchange tubes of the condenser and the steam condensate waste heat recoverer are made of 304 and 316 stainless steel.
The technical scheme of the invention has the following beneficial effects:
a. the process adopts a low-temperature heat pump evaporation technology, so that the waste heat of secondary steam and low-pressure steam condensate water is recovered to the maximum extent, and the energy utilization efficiency is improved;
b. the recovered secondary steam condensate water can be used as water supplement of the desulfurization process water, so that the overall water consumption of the desulfurization system is reduced;
c. the heater adopts a multi-channel heat exchanger, and the part with insufficient heat required by the evaporation and concentration of the desulfurization wastewater is supplemented by low-pressure steam;
d. different target concentration ratios of the desulfurization wastewater can be realized by adjusting the consumption of low-pressure steam, and the technical economy and adjustability of the evaporative crystallization process of the desulfurization wastewater are improved to the maximum extent;
e. the forced circulation evaporation process is adopted, so that the scaling problem in the evaporation concentration process of the desulfurization wastewater can be effectively prevented;
f. the heat exchange tube of the heater is made of 2205, 2507 or other higher-grade corrosion-resistant steel, so that the corrosion of the chloride ions in the desulfurization wastewater can be effectively inhibited.
Drawings
FIG. 1 is a schematic flow chart of the evaporative crystallization process of desulfurization waste water according to the present invention.
In the figure: 1-wastewater feed pump; 2-a separator; 3-forced circulation pump; 4-a heater; 5-a condenser; 6-condensation water tank; 7-a vacuum pump; 8-a condensate pump; 9-gas-liquid separator; 10-a compressor; 11-a reservoir; 12-a filter; 13-a throttle valve; 14-steam condensate water waste heat recoverer.
Detailed Description
In order to make the technical problems, technical solutions and advantages of the present invention more apparent, the following detailed description is given with reference to the accompanying drawings and specific embodiments.
Example 1
As shown in figure 1, a novel desulfurization wastewater evaporative crystallization process comprises the following steps:
step 1), desulfurization wastewater A enters a separator 2 through a wastewater feeding pump 1, then is sent into a heater 4 through a forced circulation pump 3 to be heated and absorb heat, and then enters the separator 2 to be evaporated; the desulfurization wastewater F concentrated in the separator 2 is sent into a heater 4 again through a forced circulation pump 3 to realize forced circulation evaporation, and is sent to a downstream device through a concentrated water pipeline after reaching a target concentration ratio; wherein, the desulfurization waste water exchanges heat with the wall of the refrigerant steam in the heater 4 to realize temperature rise, and enters the separator 2 to be evaporated after the temperature rise.
And 2) exchanging heat between secondary steam G generated by evaporating the desulfurization wastewater in the separator 2 and a refrigerant liquid HL partition wall in the condenser 5 to realize cooling and condensation to form secondary steam condensate E, and enabling the secondary steam condensate E to enter a condensate tank 6, wherein the secondary steam condensate E can be used as water supplement of desulfurization process water, so that the total water consumption of a desulfurization system is reduced.
Step 3), the refrigerant forms closed circulation among the condenser 5, the steam condensate waste heat recoverer 14, the gas-liquid separator 9, the compressor 10, the heater 4, the liquid accumulator 11, the filter 12 and the throttle valve 13: wherein, the liquid refrigerant HL evaporates and absorbs a large amount of heat in the condenser 5, so that the secondary steam G is cooled and condensed, the refrigerant steam is condensed in the heater 4 to release a large amount of heat, and the desulfurization wastewater is heated; the gaseous refrigerant HG enters the compressor 10 after passing through the gas-liquid separator 9, the pressure and the temperature are increased after the compression, then the gaseous refrigerant HG enters the heater 4 to release heat and condense into liquid, the desulfurization wastewater A in the heater 4 is heated, the liquid refrigerant returns to the condenser 5 after passing through the liquid accumulator 11, the filter 12 and the throttle valve 13, and the refrigerant is vaporized after absorbing heat in the condenser 5, thereby completing the refrigerant circulation.
In addition, after the secondary steam condensate water in the step 2 enters the condensate water tank 6, the non-condensable gas D and the condensate water E are respectively pumped out through a vacuum pump 7 and a condensate water pump 8. The heater 4 adopts a multi-channel heat exchanger, the part of the desulfurization wastewater which is insufficient in heat required by evaporative crystallization is supplemented by low-pressure steam B, and different target concentration ratios of the desulfurization wastewater are adjusted by adjusting the using amount of the low-pressure steam.
Example 2
The invention also provides novel desulfurization wastewater evaporative crystallization equipment, which comprises a wastewater feeding pump 1, a separator 2, a forced circulation pump 3, a heater 4, a condenser 5, a condensed water tank 6, a gas-liquid separator 9, a compressor 10, a liquid reservoir 11, a filter 12, a throttle valve 13 and a steam condensed water waste heat recoverer 14, wherein the output end of the wastewater feeding pump 1 is connected with the first wastewater input end of the separator 2, the wastewater output end of the separator 2 is connected with the wastewater input end of the heater 4 through the forced circulation pump 3, the wastewater output end of the heater 4 is connected with the second wastewater input end of the separator 2, the gas phase output end of the separator 2 is connected with the gas phase input end of the condenser 5, and the liquid phase output end of the condenser 5 is connected with the condensed water tank 6; the gas phase output end of the refrigerant of the condenser 5 is connected with a steam condensate waste heat recoverer 14, the steam condensate waste heat recoverer 14, a gas-liquid separator 9 and a compressor 10 are sequentially connected, the output end of the compressor 10 is connected with the gas phase input end of the refrigerant of the heater 4, and the liquid phase output end of the refrigerant of the heater 4 is connected with the liquid phase input end of the refrigerant of the condenser 5 sequentially through a liquid storage device 11, a filter 12 and a throttle valve 13.
The heater 4 is further connected with a steam condensate waste heat recoverer 14, and waste heat of the heater 4 can further heat a small amount of refrigerant liquid HL remaining after passing through the condenser 5, so that the refrigerant liquid HL is converted into refrigerant gas HG as much as possible and is compressed by the following compressor 10. In addition, in order to ensure safety, a gas-liquid separator 9 is connected between the steam condensate waste heat recoverer 14 and the compressor 10, so as to prevent the compressor 10 from wet operation. C in the steam condensate water graph output by the steam condensate water waste heat recoverer 14 can also be used as water supplement of desulfurization process water, and the overall water consumption of the desulfurization system is reduced.
The heater 4 is also provided with a low-pressure steam supplementing end which is connected with the output end of the low-pressure steam equipment. The part with insufficient heat required by evaporative crystallization of the desulfurization wastewater is supplemented by low-pressure steam, and different target concentration ratios of the desulfurization wastewater are adjusted by adjusting the using amount of the low-pressure steam
The output end of the condensed water tank 6 is connected with a vacuum pump 7 and a condensed water pump 8, after the secondary steam condensed water enters the condensed water tank 6, the non-condensable gas D and the condensed water E are respectively pumped out by the vacuum pump 7 and the condensed water pump 8
The heater 4 adopts a tube type heat exchanger, and the heat exchange tube material of the heater 4 adopts 2205 and 2507 steel materials. The condenser 5 adopts a tube type heat exchanger, the steam condensate waste heat recoverer 14 adopts a plate type heat exchanger, and the heat exchange tubes of the condenser 5 and the steam condensate waste heat recoverer 14 are made of 304 and 316 stainless steel.
Example 3
Take a certain 300MW coal-fired power generating unit as an example.
The unit adopts limestone-gypsum wet desulphurization, and discharges 10t of desulphurization wastewater per hour. The desulfurized wastewater was taken from the clarifier effluent supernatant and had a Total Dissolved Solids (TDS) of 41000 mg/L. The desulfurization wastewater zero-discharge project adopts a thermal method concentration and bypass flue evaporation technology. In order to effectively prevent the scaling problem caused by calcium and magnesium ions in the desulfurization wastewater in the evaporation concentration process, the target concentration multiplying power is set to be 3 times, and concentrated water is sent to a bypass flue evaporation system. The absolute pressure of the condenser is 20kPa, the initial temperature of the desulfurization waste water is 30 ℃, the low-pressure saturated steam pressure is 120kPa, and the corresponding steam temperature is 104.8 ℃. The heat load of the heater is 4.8MW, the heat load of the condenser is 4.3MW, and if the traditional single-effect evaporation technology is adopted, the low-pressure steam consumption is 7.7 t/h; if the triple effect evaporation technology is adopted, the consumption of the low-pressure steam is 2.7 t/h. By adopting the technology, the low-pressure steam consumption is only 1.0t/h, and compared with the single-effect evaporation technology, the technology can save 6.7t/h of steam per hour; the waste heat of the secondary steam and the low-pressure steam condensate can be recovered to the maximum extent, and the energy utilization efficiency is improved.
Example 4
Take a 660MW coal-fired power generation unit as an example.
The unit adopts limestone-gypsum wet desulphurization, and 20t of desulphurization wastewater is discharged every hour. The desulfurized wastewater was taken from the clarifier effluent supernatant and had a Total Dissolved Solids (TDS) of 39000 mg/L. The desulfurization wastewater zero-discharge project adopts a thermal method concentration and bypass flue evaporation technology. In order to effectively prevent the scaling problem caused by calcium and magnesium ions in the desulfurization wastewater in the evaporation concentration process, the target concentration multiplying power is set to be 4 times, and concentrated water is sent to a bypass flue evaporation system. The absolute pressure of the condenser is 20kPa, the initial temperature of the desulfurization waste water is 30 ℃, the low-pressure saturated steam pressure is 120kPa, and the corresponding steam temperature is 104.8 ℃. The heat load of the heater is 10.7MW, the heat load of the condenser is 9.7MW, and if the traditional single-effect evaporation technology is adopted, the low-pressure steam consumption is 17.2 t/h; if the triple effect evaporation technology is adopted, the consumption of the low-pressure steam is 6.0 t/h. By adopting the technology, the low-pressure steam consumption is only 2.1t/h, and compared with the single-effect evaporation technology, the technology can save 15.1t/h of steam per hour; the waste heat of the secondary steam and the low-pressure steam condensate can be recovered to the maximum extent, and the energy utilization efficiency is improved.
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (10)
1. A novel desulfurization wastewater evaporative crystallization process is characterized by comprising the following steps:
1) desulfurization wastewater enters a separator (2) through a wastewater feeding pump (1), then is sent into a heater (4) through a forced circulation pump (3) to be heated and absorb heat, and then enters the separator (2) to be evaporated; the desulfurization waste water concentrated in the separator (2) is sent into the heater (4) again through the forced circulation pump (3);
2) secondary steam generated by evaporating the desulfurization wastewater in the separator (2) exchanges heat with the liquid dividing wall of the refrigerant in the condenser (5) to realize cooling and condensation to form secondary steam condensate, and the secondary steam condensate enters the condensate water tank (6);
3) the refrigerant forms closed circulation among condenser (5), steam condensate waste heat recoverer (14), vapour and liquid separator (9), compressor (10), heater (4), reservoir (11), filter (12), choke valve (13):
wherein, the liquid refrigerant is evaporated in the condenser (5) to absorb a large amount of heat, so that the secondary steam is cooled and condensed, and the refrigerant steam is condensed in the heater (4) to release a large amount of heat, so that the desulfurization wastewater is heated;
the gaseous refrigerant enters a compressor (10) after passing through a gas-liquid separator (9), the pressure and the temperature of the gaseous refrigerant are increased after the gaseous refrigerant is compressed, the gaseous refrigerant enters a heater (4) to release heat and condense into liquid, the desulfurization wastewater in the heater (4) is heated, the liquid refrigerant returns to a condenser (5) after passing through a liquid accumulator (11), a filter (12) and a throttle valve (13), and the liquid refrigerant absorbs heat and vaporizes in the condenser (5) to complete the refrigerant circulation.
2. The novel desulfurization waste water evaporative crystallization process as defined in claim 1, wherein the desulfurization waste water in step 1) is heated in a heater (4) by heat exchange with a refrigerant steam partition wall, and the heated desulfurization waste water enters the separator (2) for evaporation.
3. The novel evaporative crystallization process for desulfurization wastewater as set forth in claim 1, wherein after the secondary steam condensate of step 2) enters the condensate tank (6), the non-condensable gas and the condensate are pumped out by a vacuum pump (7) and a condensate pump (8), respectively.
4. The novel desulfurization wastewater evaporative crystallization process as claimed in claim 1, wherein the heater (4) adopts a multi-channel heat exchanger, the part of the desulfurization wastewater which is insufficient in heat required for evaporative crystallization is supplemented by low-pressure steam, and different target concentration ratios of the desulfurization wastewater are adjusted by adjusting the amount of the low-pressure steam.
5. The novel desulfurization wastewater evaporative crystallization device for realizing the process of claim 1 is characterized by comprising a wastewater feeding pump (1), a separator (2), a forced circulation pump (3), a heater (4), a condenser (5), a condensed water tank (6), a gas-liquid separator (9), a compressor (10), a liquid reservoir (11), a filter (12), a throttle valve (13) and a steam condensed water waste heat recoverer (14), wherein the output end of the wastewater feeding pump (1) is connected with a first wastewater input end of the separator (2), the wastewater output end of the separator (2) is connected with the wastewater input end of the heater (4) through the forced circulation pump (3), the wastewater output end of the heater (4) is connected with a second wastewater input end of the separator (2), and the gas phase output end of the separator (2) is connected with the gas phase input end of the condenser (5), the liquid phase output end of the condenser (5) is connected with a condensed water tank (6);
the condenser is characterized in that a refrigerant gas phase output end of the condenser (5) is connected with a steam condensate waste heat recoverer (14), the steam condensate waste heat recoverer (14), a gas-liquid separator (9) and a compressor (10) are sequentially connected, an output end of the compressor (10) is connected with a refrigerant gas phase input end of the heater (4), and a refrigerant liquid phase output end of the heater (4) is sequentially connected with a refrigerant liquid phase input end of the condenser (5) through a liquid accumulator (11), a filter (12) and a throttle valve (13).
6. The novel desulfurization waste water evaporative crystallization apparatus of claim 5, wherein the heater (4) is further connected with a steam condensate waste heat recoverer (14).
7. The novel desulfurization waste water evaporative crystallization device of claim 5, wherein the heater (4) is further provided with a low-pressure steam supplement end, and the low-pressure steam supplement end is connected with the output end of the low-pressure steam device.
8. The novel desulfurization waste water evaporative crystallization apparatus of claim 5, wherein the output end of the condensed water tank (6) is connected with a vacuum pump (7) and a condensed water pump (8).
9. The novel desulfurization wastewater evaporative crystallization device of claim 5, wherein the heater (4) is a tube type heat exchanger, and the heat exchange tube of the heater (4) is made of 2205 and 2507 steel.
10. The novel desulfurization wastewater evaporative crystallization device of claim 5, wherein the condenser (5) adopts a tube type heat exchanger, the steam condensate waste heat recoverer (14) adopts a plate type heat exchanger, and the heat exchange tubes of the condenser (5) and the steam condensate waste heat recoverer (14) are made of 304 and 316 stainless steel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111215705.1A CN114195212A (en) | 2021-10-19 | 2021-10-19 | Novel desulfurization wastewater evaporative crystallization process and equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202111215705.1A CN114195212A (en) | 2021-10-19 | 2021-10-19 | Novel desulfurization wastewater evaporative crystallization process and equipment |
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Cited By (3)
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| CN114644378A (en) * | 2022-04-06 | 2022-06-21 | 安徽恒星世纪空调制冷设备有限公司 | Heat pump low-temperature vacuum evaporation integrated equipment for salt-containing wastewater and working method thereof |
| CN114956224A (en) * | 2022-04-11 | 2022-08-30 | 青岛宏聚环保工程有限公司 | Mechanical compression type evaporation system |
| CN115072822A (en) * | 2022-07-01 | 2022-09-20 | 国家能源集团科学技术研究院有限公司 | Desulfurization wastewater treatment system without energy consumption |
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| CN114644378A (en) * | 2022-04-06 | 2022-06-21 | 安徽恒星世纪空调制冷设备有限公司 | Heat pump low-temperature vacuum evaporation integrated equipment for salt-containing wastewater and working method thereof |
| CN114956224A (en) * | 2022-04-11 | 2022-08-30 | 青岛宏聚环保工程有限公司 | Mechanical compression type evaporation system |
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