CN207002499U - Thermal power plant's high slat-containing wastewater processing unit - Google Patents
Thermal power plant's high slat-containing wastewater processing unit Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 85
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- 239000012267 brine Substances 0.000 claims abstract description 62
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 62
- 238000002425 crystallisation Methods 0.000 claims abstract description 41
- 230000008025 crystallization Effects 0.000 claims abstract description 41
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 239000013505 freshwater Substances 0.000 claims abstract description 30
- 150000003839 salts Chemical class 0.000 claims abstract description 27
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 18
- 239000010802 sludge Substances 0.000 claims abstract description 17
- 239000013078 crystal Substances 0.000 claims abstract description 5
- 238000001223 reverse osmosis Methods 0.000 claims description 101
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 58
- 239000007788 liquid Substances 0.000 claims description 46
- 238000009292 forward osmosis Methods 0.000 claims description 45
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- 238000004062 sedimentation Methods 0.000 claims description 31
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 29
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 26
- 239000000920 calcium hydroxide Substances 0.000 claims description 26
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 26
- 239000012528 membrane Substances 0.000 claims description 23
- 238000003756 stirring Methods 0.000 claims description 19
- 150000002500 ions Chemical class 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 17
- 239000008394 flocculating agent Substances 0.000 claims description 17
- 239000003814 drug Substances 0.000 claims description 15
- 239000002253 acid Substances 0.000 claims description 10
- 238000001704 evaporation Methods 0.000 claims description 10
- 239000012153 distilled water Substances 0.000 claims description 9
- 239000002244 precipitate Substances 0.000 claims description 8
- 238000007865 diluting Methods 0.000 claims description 7
- 230000008020 evaporation Effects 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
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- 238000005516 engineering process Methods 0.000 description 4
- 239000012266 salt solution Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000008595 infiltration Effects 0.000 description 3
- 238000001764 infiltration Methods 0.000 description 3
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- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229920002125 Sokalan® Polymers 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
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- 229910021529 ammonia Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
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- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
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- 229910052749 magnesium Inorganic materials 0.000 description 1
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Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
Field of waste water treatment is the utility model is related to, discloses thermal power plant's high slat-containing wastewater processing unit.The wastewater treatment equipment includes：Wastewater Pretreatment unit (A), film upgrading unit (B) and evaporative crystallization unit (C), wherein, Wastewater Pretreatment unit (A) is used to filter thermal power plant's high slat-containing wastewater, soften, and obtains softened water and sludge；Film upgrading unit (B) is connected with Wastewater Pretreatment unit (A), for the softened water to be carried out into concentration decrement, obtains strong brine and fresh water production water；Evaporative crystallization unit (C) is connected with film upgrading unit (B), for the strong brine to be carried out into Crystallization Separation, obtains crystal salt and distillation aquatic products water.The device can reduce fouling, have the advantages of simple in construction, easy to operate, energy consumption is low, evaporated water is big, energy-conserving and environment-protective, cost of investment are low and operating cost is low.
Description
Technical Field
The utility model relates to a waste water treatment field, concretely relates to high salt effluent treatment plant that contains of thermal power plant.
Background
The zero discharge of the wastewater refers to that the salt content and pollutants in the wastewater are highly concentrated to realize fresh water recycling and solid outward transportation, and no waste liquid is discharged out of a factory. The salts and pollutants in the water are concentrated and crystallized, and are discharged in a solid form to a garbage disposal plant for landfill or are recycled as useful chemical raw materials.
At present, domestic treatment of wastewater, such as treatment of high-salt-content wastewater (represented by desulfurization wastewater, water treatment and fine treatment of regenerated wastewater) of a coal-fired power plant is still in a starting stage, domestic near-zero-emission projects of the whole plant all adopt a thermal method to treat tail end high-salt-content wastewater, and due to the fact that investment cost and operation cost are high, large-scale domestic application and popularization are not available, part of domestic coal-fired power plants adopt reverse osmosis membrane technology to treat wastewater, but reverse osmosis process is high in investment cost and operation cost, hundreds of yuan of operation cost is needed for treating 1 ton of salt-content wastewater, and no practical significance is brought to large-scale implementation. The membrane technology is adopted abroad to treat the high-salt-content wastewater, mainly focuses on the industries of garbage leachate, chemical wastewater, pharmacy and fruit juice, but the membrane technology is not related to the field of the high-salt-content wastewater of the coal-fired power plant.
The desulfurization wastewater treatment system is specially used for treating wastewater discharged by the desulfurization island. The water in the desulphurization device can be enriched with heavy metal ions and Cl in the process of continuous circulation-Ions, etc. as these ions in the slurry increase, the desulfurization system will be affected: on the one hand, the corrosion of desulfurization equipment is accelerated, and on the other hand, the quality of gypsum is influenced. Therefore, the desulfurization apparatus discharges a certain amount of wastewater, i.e., desulfurization wastewater.
In addition to the desulfurization wastewater, the main high-salt wastewater of domestic coal-fired power plants at present comprises water treatment regeneration wastewater, fine treatment regeneration wastewater, seawater desalination concentrated water and the like, and the salt content of the part of wastewater is higher than that of the desulfurization wastewater, but the heavy metal content, suspended matters, COD (chemical oxygen demand) and ammonia nitrogen are much lower than that of the desulfurization wastewater, so that the treatment is mainly concentrated and recycled.
The total salt content (TDS) of the power plant desulfurization wastewater adopting the limestone-gypsum wet desulfurization is generally 20000-30000 mg/L, and the TDSMedium chloride ion of about 10000mg/L, sulfate radical of about 2000mg/L, sodium ion of 1500-6000 mg/L, total hardness of about 10000-20000 mg/L (using CaCO)3Measured), 20000-60000 mg/L of suspended matters, and a small amount of heavy metal ions such as mercury, cadmium, lead and the like are contained in the wastewater, and if a Selective Catalytic Reduction (SCR) denitration process is equipped at the upstream of the flue gas desulfurization process, unreacted ammonia may also exist in the wastewater.
At present, the high salt-containing wastewater of a thermal power plant has the following characteristics: 1) the wastewater is weakly acidic, and the pH value is generally between 4 and 6; 2) a large amount of suspended substances, wherein the main suspended substances are gypsum particles, silicon dioxide and hydroxides of iron and aluminum; 3) the main cations in the wastewater are hardness ions such as calcium, magnesium and the like, the content is extremely high, the contents of iron, aluminum and the like are also high, and the contents of other heavy metal ions are not high, but far higher than the limit value of GB8978-1996 Integrated wastewater discharge Standard; 4) the anions in the wastewater mainly comprise Cl-，SO4 2-、SO3 2-、F-Etc., these ions are mainly derived from coal and limestone mine.
Comprehensive analysis shows that the high-salt-content wastewater of the thermal power plant has the characteristics of high salt content and high hardness, the zero-emission treatment difficulty is very high, suspended matters and salt in the wastewater are difficult to separate in the traditional process, and pure water capable of being recycled is difficult to generate. In the prior art, even if membrane concentration and crystallization technologies are adopted, the operation cost is high, the investment cost is high, the serious scaling problem exists, the energy consumption for steam, electric power and the like is quite large, energy is not saved, and the environment is not protected.
SUMMERY OF THE UTILITY MODEL
The utility model aims at overcoming the defect that current thermal power plant height contains salt effluent treatment plant and exists, providing a thermal power plant height contains salt effluent treatment plant, the device can reduce the scale deposit, have simple structure, convenient operation, the energy consumption is low, the evaporation water yield is big, energy-concerving and environment-protective, investment cost is low and running cost is low advantage.
In order to realize the above-mentioned purpose, the utility model provides a high waste water treatment device that contains salt of thermal power plant, wherein, this waste water treatment device includes: the system comprises a wastewater pretreatment unit, a membrane concentration unit and an evaporative crystallization unit, wherein the wastewater pretreatment unit is used for filtering and softening the high-salt-content wastewater of the thermal power plant to obtain softened water and sludge; the membrane concentration unit is communicated with the wastewater pretreatment unit and is used for concentrating and reducing the softened water to obtain strong brine and fresh water produced water; the evaporation crystallization unit is communicated with the membrane concentration unit and is used for carrying out crystallization separation on the strong brine to obtain crystal salt and distilled water.
Preferably, the wastewater pretreatment unit includes: the device comprises a raw water sedimentation tank, a primary softening unit, a secondary softening unit and a softening sedimentation unit; the raw water sedimentation tank is used for carrying out standing solid-liquid separation on the high-salt-content wastewater of the thermal power plant to obtain a first supernatant and a first precipitate; the primary softening unit is communicated with the raw water sedimentation tank and is used for reacting the first supernatant with a medicament containing calcium hydroxide to obtain first wastewater; the second-stage softening unit is communicated with the first-stage softening unit and is used for reacting the first wastewater with a medicament containing a flocculating agent and sodium carbonate to obtain second wastewater; the softening and precipitating unit is communicated with the secondary softening unit and is used for carrying out solid-liquid separation on the second wastewater to obtain a second supernatant and softened water and discharging the sludge.
Preferably, the primary softening unit comprises: a first-stage softening reactor, a calcium hydroxide stirring tank and a calcium hydroxide storage tank; wherein, the primary softening reactor is communicated with a raw water sedimentation tank; the calcium hydroxide stirring tank is communicated with the first-stage softening reactor and the calcium hydroxide storage tank and is used for diluting part of the second supernatant liquid with the calcium hydroxide from the calcium hydroxide storage tank and adding the diluted part of the second supernatant liquid into the first-stage softening reactor to react with the first supernatant liquid; the secondary softening unit comprises: the system comprises a secondary softening reactor, a flocculating agent stirring tank, a flocculating agent storage tank, a sodium carbonate stirring tank and a sodium carbonate storage tank; wherein, the secondary softening reactor is communicated with the primary softening reactor; the flocculant stirring tank is communicated with the secondary softening reactor and the flocculant storage tank and is used for diluting a part of the second supernatant liquid with the flocculant from the flocculant storage tank and adding the second supernatant liquid into the secondary softening reactor; and the sodium carbonate stirring tank is communicated with the secondary softening reactor and the sodium carbonate storage tank and is used for diluting part of the second supernatant liquid with the sodium carbonate from the sodium carbonate storage tank and adding the diluted part of the second supernatant liquid into the secondary softening reactor.
Preferably, the softening precipitation unit comprises: softening and precipitating tank, precipitating and concentrating tank, sludge dewatering machine and weak acid ion exchanger; the softening sedimentation tank is communicated with the secondary softening reactor and is used for carrying out sedimentation separation on the second wastewater to obtain a second supernatant and a second precipitate; the weak acid ion exchanger is communicated with the softening sedimentation tank and is used for adjusting part of the second supernatant to be neutral and removing scale to obtain softened water; and the second precipitate sequentially passes through a precipitation concentration tank and a sludge dewatering machine to become the sludge to be transported outside.
Preferably, the membrane concentration unit comprises: the device comprises a first-stage reverse osmosis unit, a second-stage reverse osmosis unit and a forward osmosis unit; the first-stage reverse osmosis unit is communicated with softened water of the wastewater pretreatment unit and is used for concentrating and reducing the softened water to obtain first-stage reverse osmosis fresh water and first-stage reverse osmosis concentrated water; the second-stage reverse osmosis unit is communicated with the first-stage reverse osmosis unit and is used for concentrating and reducing the first-stage reverse osmosis fresh water to obtain fresh water and second-stage reverse osmosis concentrated water; the forward osmosis unit is communicated with the first-stage reverse osmosis unit and the second-stage reverse osmosis unit and is used for concentrating and reducing the first-stage reverse osmosis concentrated water and the second-stage reverse osmosis concentrated water to obtain forward osmosis fresh water and concentrated brine, wherein the forward osmosis fresh water is introduced into the second-stage reverse osmosis unit for concentration and reduction.
Preferably, the primary reverse osmosis unit comprises a primary reverse osmosis water supply tank and a primary reverse osmosis device which are communicated, and softened water is introduced into the primary reverse osmosis water supply tank and then introduced into the primary reverse osmosis device for concentration and decrement; the second-stage reverse osmosis unit comprises a second-stage reverse osmosis water tank and a second-stage reverse osmosis device which are communicated, and the first-stage reverse osmosis fresh water is introduced into the second-stage reverse osmosis water tank and then is introduced into the second-stage reverse osmosis device for concentration and decrement; the forward osmosis unit comprises a forward osmosis device and a forward osmosis concentrated water tank which are communicated, the first-stage reverse osmosis concentrated water and the second-stage reverse osmosis concentrated water are introduced into the forward osmosis device for concentration and decrement to obtain forward osmosis concentrated water and forward osmosis fresh water, the forward osmosis concentrated water is introduced into the forward osmosis concentrated water tank to obtain the concentrated brine, and meanwhile, the forward osmosis fresh water is introduced into the second-stage reverse osmosis water tank.
Preferably, the evaporative crystallization unit comprises: the system comprises a strong brine buffer tank, a crystallizer, a heat exchanger and a separation crystallization unit; the strong brine buffer tank is communicated with strong brine of the membrane concentration unit and is used for buffering the strong brine to obtain the strong brine with stable pressure; the crystallizer is communicated with a strong brine buffer tank and is used for evaporating and concentrating the strong brine with stable pressure to obtain evaporated water and high-concentration brine; the heat exchanger is communicated with the crystallizer and is used for exchanging heat between the evaporated water and part of the high-concentration brine to obtain distilled water and heated high-concentration brine, and the heated high-concentration brine is circulated back to the crystallizer through a water return port in the middle of the crystallizer; the separation and crystallization unit is communicated with the crystallizer and is used for carrying out solid-liquid separation on part of high-concentration brine to obtain crystallized salt and desalted liquid.
Preferably, the separation and crystallization unit comprises: a crystallization cooling tank and a solid-liquid separator; wherein, the crystallization cooling tank is communicated with the crystallizer and is used for cooling part of the high-concentration brine to obtain cooled high-concentration brine; the solid-liquid separator is communicated with the crystallization cooling tank and is used for carrying out solid-liquid separation on the cooled high-concentration brine to obtain crystallized salt and desalted liquid.
Preferably, a demister is installed at the top of the crystallizer.
preferably, the opening angle of the crystallizer water return port and the included angle α of the inner wall of the crystallizer main body are 30-45 degrees.
According to the device, in the wastewater pretreatment unit, carbon is addedSodium, flocculating agent, calcium hydroxide, ion exchange resin, scale inhibitor and hydrochloric acid, thereby fully softening the high-salinity wastewater of the thermal power plant and effectively removing hardness ions such as Ca in the wastewater2+、Mg2+、SO4 2-、SO3 2-And the like, and heavy metal ions, provide good operating conditions for the membrane concentration unit, and can also reduce the generation of scale.
According to the device, at the concentrated unit of membrane through increasing positive osmotic engine, reduce reverse osmosis unit correspondingly, can reduce the use of high-pressure pump, greatly reduced system energy consumption, pollution abatement and scale deposit make system safe and reliable more.
Drawings
FIG. 1 is a flow chart of a high salt-containing wastewater treatment device of a thermal power plant;
FIG. 2 is a plant flow diagram of a wastewater pretreatment unit;
FIG. 3 is a flow diagram of the apparatus of the membrane concentration unit;
FIG. 4 is a flow chart of an apparatus of an evaporative crystallization unit.
Description of the reference numerals
A. Wastewater pretreatment unit B and membrane concentration unit
C. Evaporative crystallization unit I and primary softening unit
II. Two-stage softening unit III and softening precipitation unit
IV, a first-stage reverse osmosis unit V and a second-stage reverse osmosis unit
VI, a forward osmosis unit VII and a separation and crystallization unit
1. Calcium hydroxide storage tank 2 and flocculating agent storage tank
3. Sodium carbonate storage tank 4 and calcium hydroxide stirring tank
5. Flocculating agent agitator tank 6, sodium carbonate agitator tank
7. Raw water sedimentation tank 8, first-stage softening reactor
9. Second-stage softening reactor 10 and softening sedimentation tank
11. Sedimentation concentration tank 12 and sludge dewatering machine
13. Weak acid ion exchanger 14, first-stage reverse osmosis water supply tank
15. 16 primary reverse osmosis devices and two-stage reverse osmosis water tank
17. Two-stage reverse osmosis device 18 and forward osmosis device
19. A forward osmosis concentrated water tank 20 and a concentrated brine buffer tank
21. Crystallizer 22, heat exchanger
23. Crystallization cooling tank 24, solid-liquid separator
25. Demister
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The utility model provides a high waste water treatment device that contains salt of thermal power plant, as shown in figure 1, this waste water treatment device includes: the system comprises a wastewater pretreatment unit A, a membrane concentration unit B and an evaporation crystallization unit C, wherein the wastewater pretreatment unit A is used for filtering and softening the high-salt-content wastewater of the thermal power plant to obtain softened water and sludge; the membrane concentration unit B is communicated with the wastewater pretreatment unit A and is used for concentrating and reducing the softened water to obtain strong brine and fresh water produced water; and the evaporation crystallization unit C is communicated with the membrane concentration unit B and is used for carrying out crystallization separation on the strong brine to obtain crystal salt and distilled water.
In the present invention, as shown in fig. 2, the wastewater pretreatment unit a includes: a raw water sedimentation tank 7, a primary softening unit I, a secondary softening unit II and a softening sedimentation unit III.
The utility model discloses in, raw water sedimentation tank 7 is used for standing solid-liquid separation with thermal power plant's high salt waste water, obtains first supernatant and first precipitate.
The utility model discloses in, one-level softening unit I is linked together with raw water sedimentation tank 7, be used for with first supernatant reacts with the medicament that contains calcium hydroxide, obtains first waste water.
The utility model discloses in, second grade softening unit II is linked together with one-level softening unit I, be used for with first waste water reacts with the medicament that contains flocculating agent and sodium carbonate, obtains the second waste water.
The utility model discloses in, soften precipitation unit III and second grade softening unit II and be linked together, be used for with the second waste water carry out solid-liquid separation obtain the second supernatant soften water, discharge side by side mud.
In the present invention, as shown in fig. 2, the first-stage softening unit I includes: a first-stage softening reactor 8, a calcium hydroxide stirring tank 4 and a calcium hydroxide storage tank 1.
In the utility model, the one-level softening reactor 8 is communicated with the raw water sedimentation tank 7.
The utility model discloses in, calcium hydroxide agitator tank 4 is linked together with one-level softening reactor 8 and calcium hydroxide storage tank 1, is used for the part the second supernatant dilutes the calcium hydroxide that comes from calcium hydroxide storage tank 1 to add in one-level softening reactor 8 with first supernatant reacts.
In the present invention, as shown in fig. 2, the second softening unit II includes: a secondary softening reactor 9, a flocculant stirring tank 5, a flocculant storage tank 2, a sodium carbonate stirring tank 6 and a sodium carbonate storage tank 3.
In the utility model, the second-stage softening reactor 9 is communicated with the first-stage softening reactor 8.
The utility model discloses in, flocculating agent agitator tank 5 is linked together with second grade softening reactor 9 and flocculating agent storage tank 2, is used for the part the second supernatant dilutes the flocculating agent that comes from flocculating agent storage tank 2 to add second grade softening reactor 9.
According to the present invention, the flocculant may be an organic or inorganic flocculant conventional in the art, and preferably, the flocculant is one or more of polyaluminium chloride, polyaluminium sulfate, polyferric chloride and polyferric sulfate.
The utility model discloses in, sodium carbonate agitator tank 6 is linked together with second grade softening reactor 9 and sodium carbonate storage tank 3 for with the part the second supernatant dilutes the sodium carbonate that comes from sodium carbonate storage tank 3 to add second grade softening reactor 9. The sodium carbonate can reduce the occurrence of scale formation and meet the requirement of forward osmosis on the wastewater to be treated.
The utility model discloses in, the medicament in the flocculating agent agitator tank 5 can add second grade softening reactor 9 jointly after mixing with the medicament in the sodium carbonate agitator tank 6, perhaps second grade softening reactor 9 is added respectively to the medicament in the flocculating agent agitator tank 5 and the medicament in the sodium carbonate agitator tank 6. In the preferred condition of the utility model, the second grade softening reactor 9 is added respectively to the medicament in the flocculating agent agitator tank 5 and the medicament in the sodium carbonate agitator tank 6.
In the present invention, as shown in fig. 2, the softening and precipitating unit III includes: softening and settling tank 10, settling and concentrating tank 11, sludge dewatering machine 12 and weak acid ion exchanger 13.
The utility model discloses in, soften sedimentation tank 10 and second grade and soften reactor 9 and be linked together, be used for with the second waste water carries out the sedimentation separation, obtains second supernatant and second precipitate. And (3) according to the dilution requirement, part of the second supernatant enters a calcium hydroxide stirring tank 4, a flocculating agent stirring tank 5 and a sodium carbonate stirring tank 6, and is used for diluting the medicament in the calcium hydroxide storage tank 1, the medicament in the flocculating agent storage tank 2 and the medicament in the sodium carbonate storage tank 3. A portion of the second supernatant enters the weak acid ion exchanger 13.
In the present invention, the weak acid ion exchanger 13 is connected to the softening and settling tank 10 for adjusting the second supernatant to neutral and removing scale to obtain the softened water.
Preferably, the weak acid ion exchanger 13 is filled with a liquid containing an ion exchange resin, hydrochloric acid and a scale inhibitor. The weak acid ion exchanger 13 can effectively reduce the hardness in the wastewater, reduce the structure of the device and ensure the safe and stable operation of the reverse osmosis device and the forward osmosis device.
According to the utility model discloses, the antisludging agent can be one or more in PBTCA, polyacrylic acid PAA and multipolymer.
The utility model discloses in, the second precipitate becomes behind sedimentation concentration tank 11, sludge dewaterer 12 in proper order sludge is outward transported. Wherein, the second sediment is precipitated and separated in the precipitation concentration tank 11, the third supernatant obtained by separation enters the raw water sedimentation tank 7, and the third sediment obtained by separation enters the sludge dewatering machine 12.
In the present invention, as shown in fig. 3, the membrane concentration unit B includes: a first-stage reverse osmosis unit IV, a second-stage reverse osmosis unit V and a forward osmosis unit VI.
The utility model discloses in, one-level reverse osmosis unit IV communicates with the softened water phase of wastewater pretreatment unit A, be used for with the concentrated decrement of demineralized water obtains one-level reverse osmosis fresh water and the dense water of one-level reverse osmosis.
The utility model discloses in, second grade reverse osmosis unit V is linked together with one-level reverse osmosis unit IV, be used for with one-level reverse osmosis fresh water carries out the concentrated decrement, obtains fresh water product and the dense water of second grade reverse osmosis.
The utility model discloses in, positive infiltration unit VI is linked together with one-level reverse osmosis unit IV, second grade reverse osmosis unit V, be used for with the concentrated water of one-level reverse osmosis with the concentrated water of second grade reverse osmosis carries out concentrated decrement, obtains the fresh water of positive infiltration and the concentrated water of positive infiltration.
In the utility model, the forward osmosis fresh water is introduced into the second-stage reverse osmosis unit V for concentration and decrement.
The utility model discloses in, as shown in fig. 3, one-level reverse osmosis unit IV is including the one-level reverse osmosis feedwater water tank 14 and the one-level reverse osmosis unit 15 that are linked together, the demineralized water lets in behind the one-level reverse osmosis feedwater water tank 14 rethread one-level reverse osmosis unit 15 and carries out the concentration decrement. The primary reverse osmosis feed water tank 14 may buffer the primary reverse osmosis unit I and provide a source of water for the high pressure water pump. After the first-stage reverse osmosis and/or the second-stage reverse osmosis, a pump with higher pressure is generally required to be used, however, the forward osmosis device does not need a high-pressure pump, can also effectively remove dissolved salts in the wastewater, and has the advantage of low energy consumption of the system.
The utility model discloses in, second grade reverse osmosis unit V is including the second grade reverse osmosis water tank 16 and the second grade reverse osmosis unit 17 that are linked together, the one-level reverse osmosis fresh water lets in behind the second grade reverse osmosis water tank 16 rethread second grade reverse osmosis unit 17 and carries out the concentration decrement. The secondary reverse osmosis water tank 16 may buffer the secondary reverse osmosis unit II and provide a water source for the high pressure water pump.
The forward osmosis unit VI comprises a forward osmosis device 18 and a forward osmosis concentrated water tank 19 which are communicated, the first-stage reverse osmosis concentrated water and the second-stage reverse osmosis concentrated water are introduced into the forward osmosis device 18 for concentration and decrement to obtain forward osmosis concentrated water and forward osmosis fresh water, the forward osmosis concentrated water is introduced into the forward osmosis concentrated water tank 19 to obtain the concentrated water, and meanwhile, the forward osmosis fresh water is introduced into the second-stage reverse osmosis water tank 16. Contain the pellicle and draw the liquid in the forward osmosis unit, forward osmosis membrane irreversible pollution and scale deposit tendency are lower than high pressure reverse osmosis system, and the system is more reliable, and the device is energy-concerving and environment-protective more.
In the present invention, as shown in fig. 4, the evaporative crystallization unit C includes: a concentrated brine buffer tank 20, a crystallizer 21, a heat exchanger 22 and a separation and crystallization unit VII.
The utility model discloses in, strong brine buffer tank 20 is linked together with evaporation crystal unit B's strong brine, be used for with the strong brine cushions, obtains the steady strong brine of pressure.
The utility model discloses in, crystallizer 21 is linked together with strong brine buffer tank 20, be used for with the strong brine evaporative concentration that pressure is steady obtains evaporating water and high concentration salt solution.
The utility model discloses in, heat exchanger 22 is linked together with crystallizer 21, be used for with evaporating water and part high concentration salt solution carries out heat exchange, obtains distilled water product and the high concentration salt solution of heating, and the high concentration salt solution of heating passes through the return water mouth circulation return crystallizer 21 at crystallizer 21 middle part.
The heat exchanger 22 may be any of a variety of heat exchangers conventional in the art. In the preferred aspect of the present invention, the heat exchanger 22 is a shell and tube heat exchanger.
In a preferable case, a tube-side inlet of the heat exchanger 22 is communicated with a water outlet pipe of the high-concentration brine at the bottom of the crystallizer 21, a tube-side outlet of the heat exchanger 22 is connected with a water return port at the middle part of the crystallizer 21, a shell-side inlet of the heat exchanger 22 is communicated with an evaporated water outlet at the top of the crystallizer 21, and a shell-side outlet of the heat exchanger 22 discharges distilled water to produce water. In the heat exchanger 22, the evaporated water at the top of the crystallizer 21 is cooled in the heat exchanger 22, heat is released and discharged as distilled water product water, and the high-concentration brine at the bottom of the crystallizer 21 absorbs heat and then circulates back to the inside of the crystallizer 21. The heat of the steam is used as a heat source of the crystallization heater, so that the use amount of the steam is reduced, and the energy consumption is reduced. The distilled water can be recycled by enterprises, so that the waste water is utilized, the consumption of fresh water resources is reduced, and the energy is saved and the environment is protected.
In the utility model, the separation and crystallization unit VII is communicated with the crystallizer 21 and is used for carrying out solid-liquid separation on partial high-concentration brine to obtain crystallized salt and desalted liquid.
In the present invention, the separation and crystallization unit VII includes: a crystallization cooling tank 23 and a solid-liquid separator 24.
In the present invention, the crystallization cooling tank 23 is connected to the crystallizer 21 for cooling part of the high concentration brine to obtain cooled high concentration brine.
According to the present invention, the crystallization cooling tank 23 may be any of various conventional cooling tanks in the art. Preferably, the crystallization cooling tank 23 is a coil cooling tank.
In the present invention, the solid-liquid separator 24 is communicated with the crystallization cooling tank 23 for performing solid-liquid separation of the cooled high concentration brine to obtain crystallized salt and desalted liquid.
In accordance with the present invention, solid-liquid separator 24 can be any of a variety of conventional solid-liquid separators known in the art. Preferably, the solid-liquid separator 24 is a centrifuge or a filter. It is further preferred that a hydrocyclone is used before the centrifuge to increase the concentration of the magma.
In order to deeply separate the gas with liquid or liquid droplets and remove the attached particles, a demister 25 is preferably installed at the top of the crystallizer 21. The demister 25 is a demister that is conventional in the art, and is not particularly limited so long as it can achieve deep separation.
in a preferable case, in order to facilitate the heated high-concentration brine to circulate back into the main body of the crystallizer 21, an angle α formed by an opening angle of a water return port of the crystallizer 21 and an inner wall of the main body of the crystallizer is 30 ° to 45 °.
Preferably, a compressor is provided between the outlet at the top of the crystallizer 21 and the heat exchanger 22 for heating the evaporated water at the top of the crystallizer 21, reducing the possibility of the structure inside the tubes. Preferably, the compressor is a mechanical vapor compressor. The mechanical vapor compressor utilizes the heat generated by evaporated water, the pressure and the temperature are increased through the compression action, the enthalpy is increased, the thermal efficiency is improved, the high flow speed of the waste water in the heater is ensured, and the possibility of scaling in the pipe is reduced. In the operation process, raw steam is required to be introduced to heat liquid in the evaporator when the equipment is started, so that waste water can be heated and evaporated, and only a compressor and a heat exchanger are required to maintain heat required by the system when the system stably runs.
Preferably, a pump is disposed between the brine buffer tank 20 and the crystallizer 21 for pumping the brine in the brine buffer tank 20 into the crystallizer 21.
Preferably, a strong brine circulating pump is provided between the outlet of the bottom of the crystallizer 21 and the heat exchanger 22 for pumping the high concentration brine to the inside of the heat exchanger 22.
Preferably, a concentration detector or a specific gravity detector is provided at the outlet of the crystallizer 21 in order to detect the concentration of the concentrated brine. Preferably, the detector is a real-time on-line detector.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. In the technical idea scope of the present invention, it can be right to the technical solution of the present invention perform multiple simple modifications, including each technical feature combined in any other suitable manner, these simple modifications and combinations should be regarded as the disclosed content of the present invention, and all belong to the protection scope of the present invention.
Claims (10)
1. The utility model provides a high salt effluent treatment plant that contains of thermal power plant which characterized in that, this effluent treatment plant includes: a wastewater pretreatment unit (A), a membrane concentration unit (B) and an evaporative crystallization unit (C), wherein,
the wastewater pretreatment unit (A) is used for filtering and softening the high-salt-content wastewater of the thermal power plant to obtain softened water and sludge;
the membrane concentration unit (B) is communicated with the wastewater pretreatment unit (A) and is used for concentrating and reducing the softened water to obtain strong brine and fresh water produced water;
and the evaporation crystallization unit (C) is communicated with the membrane concentration unit (B) and is used for carrying out crystallization separation on the strong brine to obtain crystal salt and distilled water.
2. The wastewater treatment plant according to claim 1, characterized in that the wastewater pretreatment unit (a) comprises: a raw water sedimentation tank (7), a primary softening unit (I), a secondary softening unit (II) and a softening sedimentation unit (III); wherein,
the raw water sedimentation tank (7) is used for carrying out standing solid-liquid separation on the high-salt-content wastewater of the thermal power plant to obtain a first supernatant and a first precipitate;
the primary softening unit (I) is communicated with the raw water sedimentation tank (7) and is used for reacting the first supernatant with a medicament containing calcium hydroxide to obtain first wastewater;
the second-stage softening unit (II) is communicated with the first-stage softening unit (I) and is used for reacting the first wastewater with a medicament containing a flocculating agent and sodium carbonate to obtain second wastewater;
and the softening and precipitating unit (III) is communicated with the secondary softening unit (II) and is used for carrying out solid-liquid separation on the second wastewater to obtain a second supernatant, softened water and discharging the sludge.
3. Wastewater treatment plant according to claim 2, characterized in that the primary softening unit (I) comprises: a first-stage softening reactor (8), a calcium hydroxide stirring tank (4) and a calcium hydroxide storage tank (1); wherein, the primary softening reactor (8) is communicated with the raw water sedimentation tank (7);
the calcium hydroxide stirring tank (4) is communicated with the first-stage softening reactor (8) and the calcium hydroxide storage tank (1) and is used for diluting part of the second supernatant liquid with the calcium hydroxide from the calcium hydroxide storage tank (1) and adding the diluted part of the second supernatant liquid into the first-stage softening reactor (8) to react with the first supernatant liquid;
the secondary softening unit (II) comprises: a secondary softening reactor (9), a flocculant stirring tank (5), a flocculant storage tank (2), a sodium carbonate stirring tank (6) and a sodium carbonate storage tank (3); wherein, the secondary softening reactor (9) is communicated with the primary softening reactor (8);
the flocculant stirring tank (5) is communicated with the secondary softening reactor (9) and the flocculant storage tank (2) and is used for diluting a part of the second supernatant liquid with the flocculant from the flocculant storage tank (2) and adding the part of the second supernatant liquid into the secondary softening reactor (9);
wherein the sodium carbonate stirring tank (6) is communicated with the secondary softening reactor (9) and the sodium carbonate storage tank (3) and is used for diluting part of the second supernatant fluid with the sodium carbonate from the sodium carbonate storage tank (3) and adding the diluted part of the second supernatant fluid into the secondary softening reactor (9).
4. The wastewater treatment plant according to claim 2, characterized in that the softening-precipitation unit (III) comprises: a softening sedimentation tank (10), a sedimentation concentration tank (11), a sludge dewatering machine (12) and a weak acid ion exchanger (13);
the softening sedimentation tank (10) is communicated with the secondary softening reactor (9) and is used for carrying out sedimentation separation on the second wastewater to obtain a second supernatant and a second precipitate;
the weak acid ion exchanger (13) is communicated with the softening sedimentation tank (10) and is used for adjusting part of the second supernatant to be neutral and removing scale to obtain softened water;
and the second sediment passes through a sedimentation concentration tank (11) and a sludge dewatering machine (12) in sequence and becomes the sludge to be transported outside.
5. The wastewater treatment plant according to claim 1, characterized in that the membrane concentration unit (B) comprises: a primary reverse osmosis unit (IV), a secondary reverse osmosis unit (V) and a forward osmosis unit (VI); wherein,
the primary reverse osmosis unit (IV) is communicated with the softened water of the wastewater pretreatment unit (A) and is used for concentrating and reducing the softened water to obtain primary reverse osmosis fresh water and primary reverse osmosis concentrated water;
the second-stage reverse osmosis unit (V) is communicated with the first-stage reverse osmosis unit (IV) and is used for concentrating and reducing the first-stage reverse osmosis fresh water to obtain fresh water and second-stage reverse osmosis concentrated water;
and the forward osmosis unit (VI) is communicated with the first-stage reverse osmosis unit (IV) and the second-stage reverse osmosis unit (V) and is used for concentrating and reducing the first-stage reverse osmosis concentrated water and the second-stage reverse osmosis concentrated water to obtain forward osmosis fresh water and concentrated brine, wherein the forward osmosis fresh water is introduced into the second-stage reverse osmosis unit (V) for concentration and reduction.
6. The wastewater treatment device according to claim 5, wherein the primary reverse osmosis unit (IV) comprises a primary reverse osmosis feed water tank (14) and a primary reverse osmosis device (15) which are communicated with each other, and softened water is introduced into the primary reverse osmosis feed water tank (14) and then introduced into the primary reverse osmosis device (15) for concentration and decrement;
the secondary reverse osmosis unit (V) comprises a secondary reverse osmosis water tank (16) and a secondary reverse osmosis device (17) which are communicated, and the primary reverse osmosis fresh water is introduced into the secondary reverse osmosis water tank (16) and then introduced into the secondary reverse osmosis device (17) for concentration and decrement;
the forward osmosis unit (VI) comprises a forward osmosis device (18) and a forward osmosis concentrated water tank (19) which are communicated, the first-stage reverse osmosis concentrated water and the second-stage reverse osmosis concentrated water are introduced into the forward osmosis device (18) to be concentrated and reduced to obtain forward osmosis concentrated water and forward osmosis fresh water, the forward osmosis concentrated water is introduced into the forward osmosis concentrated water tank (19) to obtain the concentrated water, and meanwhile, the forward osmosis fresh water is introduced into the second-stage reverse osmosis water tank (16).
7. The wastewater treatment plant according to claim 1, characterized in that said evaporative crystallization unit (C) comprises: a strong brine buffer tank (20), a crystallizer (21), a heat exchanger (22) and a separation crystallization unit (VII); wherein,
the strong brine buffer tank (20) is communicated with the strong brine of the membrane concentration unit (B) and is used for buffering the strong brine to obtain the strong brine with stable pressure;
the crystallizer (21) is communicated with a strong brine buffer tank (20) and is used for evaporating and concentrating the strong brine with stable pressure to obtain evaporated water and high-concentration brine;
the heat exchanger (22) is communicated with the crystallizer (21) and is used for exchanging heat between the evaporated water and part of the high-concentration brine to obtain distilled water and heated high-concentration brine, and the heated high-concentration brine is circulated back to the crystallizer (21) through a water return port in the middle of the crystallizer (21);
the separation and crystallization unit (VII) is communicated with the crystallizer (21) and is used for carrying out solid-liquid separation on part of high-concentration brine to obtain crystallized salt and desalted liquid.
8. Wastewater treatment plant according to claim 7, characterized in that said separation and crystallization unit (VII) comprises: a crystallization cooling tank (23) and a solid-liquid separator (24); wherein,
the crystallization cooling tank (23) is communicated with the crystallizer (21) and is used for cooling part of high-concentration brine to obtain cooled high-concentration brine;
the solid-liquid separator (24) is communicated with the crystallization cooling tank (23) and is used for carrying out solid-liquid separation on the cooled high-concentration brine to obtain crystallized salt and desalted liquid.
9. The wastewater treatment plant according to claim 7, characterized in that a demister (25) is installed at the top of the crystallizer (21).
10. the wastewater treatment device according to claim 7, characterized in that the opening angle of the water return port of the crystallizer (21) and the included angle alpha of the inner wall of the crystallizer main body are 30-45 degrees.
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