CN106082514A - Desulfuration waste water treatment process and processing means thereof - Google Patents
Desulfuration waste water treatment process and processing means thereof Download PDFInfo
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- CN106082514A CN106082514A CN201610467661.4A CN201610467661A CN106082514A CN 106082514 A CN106082514 A CN 106082514A CN 201610467661 A CN201610467661 A CN 201610467661A CN 106082514 A CN106082514 A CN 106082514A
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- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 19
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 11
- 230000000694 effects Effects 0.000 claims abstract description 194
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 123
- 239000002351 wastewater Substances 0.000 claims abstract description 64
- 238000005345 coagulation Methods 0.000 claims abstract description 49
- 230000015271 coagulation Effects 0.000 claims abstract description 49
- 239000006200 vaporizer Substances 0.000 claims abstract description 36
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 16
- 230000023556 desulfurization Effects 0.000 claims abstract description 11
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000000126 substance Substances 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims description 118
- 238000001704 evaporation Methods 0.000 claims description 108
- 230000008020 evaporation Effects 0.000 claims description 108
- 238000000926 separation method Methods 0.000 claims description 88
- 239000000243 solution Substances 0.000 claims description 64
- 238000003756 stirring Methods 0.000 claims description 28
- 239000012153 distilled water Substances 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 239000012267 brine Substances 0.000 claims description 17
- 150000003839 salts Chemical class 0.000 claims description 17
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 15
- 238000004821 distillation Methods 0.000 claims description 15
- 238000001556 precipitation Methods 0.000 claims description 15
- 238000002425 crystallisation Methods 0.000 claims description 14
- 230000008025 crystallization Effects 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 14
- 239000007787 solid Substances 0.000 claims description 14
- 238000009833 condensation Methods 0.000 claims description 13
- 230000005494 condensation Effects 0.000 claims description 13
- 229920002401 polyacrylamide Polymers 0.000 claims description 13
- 239000013078 crystal Substances 0.000 claims description 12
- 239000013049 sediment Substances 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 11
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 10
- 230000018044 dehydration Effects 0.000 claims description 10
- 238000006297 dehydration reaction Methods 0.000 claims description 10
- 239000002244 precipitate Substances 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 5
- 238000010025 steaming Methods 0.000 claims description 4
- 238000009834 vaporization Methods 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 3
- 241000628997 Flos Species 0.000 claims description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 3
- 239000004411 aluminium Substances 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 230000001112 coagulating effect Effects 0.000 claims description 3
- 238000005189 flocculation Methods 0.000 claims description 3
- 230000016615 flocculation Effects 0.000 claims description 3
- 239000011541 reaction mixture Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 239000000725 suspension Substances 0.000 claims description 3
- 239000010786 composite waste Substances 0.000 claims description 2
- 239000011148 porous material Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 14
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 239000003814 drug Substances 0.000 description 4
- 235000017550 sodium carbonate Nutrition 0.000 description 4
- 239000010440 gypsum Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- 229910001424 calcium ion Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 2
- 239000001095 magnesium carbonate Substances 0.000 description 2
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- QWDJLDTYWNBUKE-UHFFFAOYSA-L magnesium bicarbonate Chemical compound [Mg+2].OC([O-])=O.OC([O-])=O QWDJLDTYWNBUKE-UHFFFAOYSA-L 0.000 description 1
- 229910000022 magnesium bicarbonate Inorganic materials 0.000 description 1
- 239000002370 magnesium bicarbonate Substances 0.000 description 1
- 235000014824 magnesium bicarbonate Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 239000010802 sludge 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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
-
- 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
Landscapes
- 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)
Abstract
The present invention discloses and provide a kind of, and technology chain is short, added amount of chemical is few, operating cost is cheap, stable water outlet qualified discharge and can accomplish effluent reuse thus save desulfuration waste water treatment process and the processing means thereof of water resource.Wherein desulfurizing waste water processing device includes coagulation pretreatment device, low energy consumption MVR vaporizer (1) and triple effect concentrated solution forced circulation crystallizer (23), described coagulation pretreatment device, described low energy consumption MVR vaporizer (1) and described triple effect concentrated solution forced circulation crystallizer (23) are sequentially connected and connect, and described coagulation pretreatment device is connected with outside waste water water tank.The present invention is applicable to power plant desulfurization field of waste water treatment.
Description
Technical field
The present invention relates to a kind of desulfuration waste water treatment process and processing means thereof.
Background technology
The wastewater source that power-plant flue gas wet desulphurization limestone/gypsum method process produces is in the discharge water on absorption tower.In order to
Maintain the balance of desulfurizer serum recycle system material, prevent soluble fraction i.e. cl concn in flue gas from exceeding setting and guarantee
Gypsum quality, it is necessary to discharge a certain amount of waste water from system, waste water is essentially from gypsum dehydration and purging system.Waste water contains
Some impurity mainly includes float, oversaturated sulphite, sulfate and heavy metal, is the most much national environmental protection mark
Standard requires the strict first kind pollutant controlled.Prior art is mainly simply located by the method for physics and chemistry
Reason, needs to add a large amount of medicament to remove the pollutant such as the float inside waste water and heavy metal, and dosage is big, technique chain length,
Operating cost is high；Again since it is desired that feeding lime, medicament configures and adds process complexity, and the amount of labour of workman is big, the dirt of generation
Mud amount is relatively big, and sludge treatment is costly；Again because the defect of technique itself, effluent quality is unstable, can reach three grades of rows reluctantly
Put standard, it is impossible to reach waste water recycling and the purpose of using water wisely resource.And owing to the salt of water outlet is the most effectively gone
Remove, therefore limit the possibility of waste water recycling.
Summary of the invention
The technical problem to be solved is to overcome the deficiencies in the prior art, it is provided that a kind of technology chain is short, medicament is thrown
Dosage is few, operating cost is cheap, stable water outlet qualified discharge and can accomplish effluent reuse thus save the desulfurization of water resource
Waste water treatment process and processing means thereof.
The technical solution adopted in the present invention is: a kind of desulfurizing waste water processing device, it include coagulation pretreatment device,
MVR vaporizer and triple effect concentrated solution forced circulation crystallizer, described coagulation pretreatment device, described MVR vaporizer and institute
Stating triple effect concentrated solution forced circulation crystallizer to be sequentially connected and connect, described coagulation pretreatment device is connected with outside waste water water tank.
Described coagulation pretreatment device includes being sequentially connected one-level stirring coagulation case, one-level settling tank, the two grades of stirrings connect
Coagulation case, two-stage precipitation case and intermediate reaction case, described one-level stirring coagulation case with outside waste water water tank be connected, described in
Between the outlet of reaction chamber be connected with the water inlet of described MVR vaporizer, described coagulation pretreatment device also includes dewaterer,
The charging aperture of described dewaterer discharging opening with the discharging opening of described one-level settling tank and described two-stage precipitation case respectively is connected
Connect.
Described triple effect concentrated solution forced circulation crystallizer includes the first effect heating evaporation room, the first effect separation chamber, the second effect
Heating evaporation room, the second effect separation chamber, triple effect heating evaporation room, triple effect separation chamber, final condenser, final Crystallization Separation
Machine and distillation water pot, the water inlet of described first effect heating evaporation room is connected with the leakage fluid dram of described MVR vaporizer, described
The outlet of the first effect heating evaporation room is connected with the water inlet of described first effect separation chamber, and described first effect separation chamber goes out
The mouth of a river is connected with the water inlet of described second effect heating evaporation room, the outlet and described the of described second effect heating evaporation room
The water inlet of two effect separation chambers is connected, the outlet of described second effect separation chamber and the water inlet of described triple effect heating evaporation room
Mouthful being connected, the described outlet of triple effect heating evaporation room is connected with the water inlet of described triple effect separation chamber, and described the
The discharging opening of triple effect separation chamber is connected with the charging aperture of described final Crystallization Separation machine, entering of described first effect heating evaporation room
QI KOU is connected with outside saturated vapor source, the gas outlet of described first effect heating evaporation room, described second effect heating evaporation room
Gas outlet and the gas outlet air inlet with described final condenser respectively of described triple effect heating evaporation room be connected, institute
The gas outlet stating final condenser connects outer exhaust duct group 22, and described second effect heating evaporation room, the heating of described triple effect are steamed
Send out room and described final condenser be provided with distilled water discharging mouth and respectively water inlet with described distillation water pot be connected.
Described first effect separation chamber, described second effect separation chamber and described triple effect separation chamber are provided with dope backflow
Mouth and venthole, the dope refluxing opening of described first effect separation chamber and the water inlet of described first effect heating evaporation room are connected
Connecing, the dope refluxing opening of described second effect separation chamber is connected with the water inlet of described second effect heating evaporation room, and the described 3rd
The dope refluxing opening of effect separation chamber is connected with the water inlet of described triple effect heating evaporation room, and described first effect separation chamber goes out
Pore is connected with the air inlet of described second effect heating evaporation room, the venthole of described second effect separation chamber and described triple effect
The air inlet of heating evaporation room is connected, and the venthole of described triple effect separation chamber is connected with the air inlet of described final condenser
Connect.
Described desulfurizing waste water processing device also includes heat exchanger group and condensate water pot, the water inlet of described condensate water pot
It is connected with the distilled water discharging mouth of described first effect heating evaporation room, the outlet of described condensate water pot and described heat exchanger
The condensed water water inlet of group is connected, and the gas outlet of described condensate water pot is connected with the air inlet of described first effect heating evaporation room
Connecing, the outlet of described distillation water pot is connected with the distilled water water inlet of described heat exchanger group, described heat exchanger group
Distilled water outlet tank up to standard with outside is connected, and described heat exchanger group is additionally provided with strong brine import and dense salt
Water out, described strong brine import is connected with the strong brine floss hole of described MVR vaporizer, and described brine outlet is with described
The strong brine recovery port of MVR vaporizer is connected.
A kind of desulfuration waste water treatment process realized by above-mentioned desulfurizing waste water processing device, it is characterised in that: its bag
Include following steps:
A. desulfurization wastewater is carried out pretreatment:
A. desulfurization wastewater is pumped to described one-level stirring coagulation case, adds PAM in stirring coagulation case toward described one-level (poly-simultaneously
Acrylamide) and stir, make PAM (polyacrylamide) become greatly with the float generation flocculation reaction in waste water thus conglomeration；
B. precipitate and separate, precipitate and separate are carried out in the waste water reaction mixture produced in step a being delivered to described one-level settling tank
After the supernatant that obtains deliver to described two grades of stirring coagulation casees, after separation, the solid sediment of gained is delivered to described dewaterer and is carried out
It is dehydrated to water content less than 60%, then processes making outward transport after the solid sediment pack after dehydration；
C. add sodium carbonate and make it be sufficiently mixed with waste water in tank in described two grades of stirring coagulation casees；
The most respectively toward throwing in aluminium polychlorid (PAC) and polyacrylamide (PAM) in described two grades of stirring coagulation casees, further with
Fine suspension and colloidal substance in waste water produce coagulating, and by adsorption bridging effect, conglomeration becomes big and is prone to precipitation；
E. precipitation point is carried out in the composite waste in described in step d two grades of stirring coagulation casees being delivered to described two-stage precipitation case
From, after precipitate and separate, the supernatant of gained is delivered to described intermediate reaction case, and after separation, the solid sediment of gained is delivered to institute
State dewaterer to carry out being dehydrated and process less than 60% and by making outward transport after packed for the solid sediment after dehydration to moisture content；
F. in described intermediate reaction case, dilute hydrochloric acid is thrown in so that the pH value of the waste water in described intermediate reaction case is reduced to 5.5
And between 6.5, eliminate the impact of remaining carbonate in waste water；
B., the waste water of last for step A gained is delivered to described MVR vaporizer, and waste water is decomposed into and does not coagulate by described MVR vaporizer
Gas, distilled water and concentrated solution, wherein on-condensible gas is emitted into outside by pipe group, and distilled water is collected to described MVR evaporation
Outer row after device internal distillation water pot；
C. the concentrated solution produced in step B is carried out triple effect forced circulation crystallization treatment:
In the concentrated solution that the most described MVR vaporizer is produced is delivered to described heat exchanger group and with from described condensate water pot
The condensed water discharged carries out heat exchange, and after completing, concentrated solution is transported to described triple effect concentrated solution forced circulation crystallizer；
H. complete the concentrated solution of heat exchange to be transported to described first effect heating evaporation indoor and carry out heating evaporation and decomposite secondary
Concentrated solution and water vapour, wherein water vapour is transported to described final condenser and carries out condensation process, and secondary concentration liquid is carried
Separating to described first effect separation chamber, in separation process, part secondary concentration liquid is back to described first effect heating evaporation
Indoor proceed heating evaporation, another part secondary concentration liquid and the effect steam decomposited and are transported to institute the most respectively
State the second effect heating evaporation room carry out heating evaporation decomposite three concentrated solutions and two effect steam, wherein two effect water vapour defeated
Delivering to described final condenser and carry out condensation process, three concentrated solutions are transported to described second effect separation chamber and separate, point
During from, portion's concentrated solution in three times is back to described second effect heating evaporation room and proceeds heating evaporation；
I. three concentrated solutions of the another part in step h and two effect steam are transported to the heating steaming of described triple effect the most respectively
Sending out indoor and carry out heating evaporation, thus decomposite four concentrated solutions and triple effect water vapour, wherein triple effect steam is transported to institute
Stating final condenser and carry out condensation process, four concentrated solutions are transported to described triple effect separation chamber and carry out Crystallization Separation, separate
During isolate crystal salt and four concentrated solutions of residue, wherein four concentrated solutions of residue are back to the heating of described triple effect and steam
Sending out room and proceed heating evaporation, the steam in described three separation chambers is transported to described final condenser to be carried out at condensation
Reason, and crystal salt carries out last water salt and separates in being sent to described final Crystallization Separation machine, and final sub-argument goes out final crystal salt
And five concentrated solutions, wherein five concentrated solutions are back to described triple effect heating evaporation room and proceed heating evaporation, and
Whole crystal salt is transported outward process.
In step C, described first effect heating evaporation room, described second effect heating evaporation room and the heating of described triple effect
The distilled water produced in vaporization chamber is transported to described distillation water pot respectively, then is delivered to outside up to standard through described heat exchanger group
Tank.
The invention has the beneficial effects as follows: in the present invention, due to have employed coagulation pretreatment device, MVR vaporizer and
Desulfurization wastewater is successively repeatedly evaporated and concentration by triple effect concentrated solution forced circulation crystallizer, so that desulfurization is given up
Water can after treatment can qualified discharge even zero-emission, simultaneously relative to conventional technique, the technology chain journey of the present invention is more
Terse, medicine throwing amount is less, operating cost is cheaper, additionally it is possible to recycle-water resource.
Accompanying drawing explanation
Fig. 1 is the overall structure connection diagram of desulfurizing waste water processing device in the present invention；
Fig. 2 is the structure connection diagram of the triple effect concentrated solution forced circulation crystallizer of desulfurizing waste water processing device in the present invention.
Detailed description of the invention
As shown in Figure 1 and Figure 2, a kind of desulfurizing waste water processing device, it include coagulation pretreatment device, MVR vaporizer 1 with
And triple effect concentrated solution forced circulation crystallizer 23, described coagulation pretreatment device, described MVR vaporizer 1 and described triple effect are dense
Contracting liquid forced circulation crystallizer 23 is sequentially connected and connects, and described coagulation pretreatment device is connected with outside waste water water tank.
Described coagulation pretreatment device includes coagulation pretreatment device, MVR vaporizer 1 and triple effect concentrated solution forced circulation
Crystallizer 23, described coagulation pretreatment device, described MVR vaporizer 1 and described triple effect concentrated solution forced circulation crystallizer 23
Being sequentially connected and connect, described coagulation pretreatment device is connected with outside waste water water tank.
Described coagulation pretreatment device includes being sequentially connected the one-level stirring coagulation case 2 that connects, one-level settling tank 3, two grades stirs
Mixing coagulation case 4, two-stage precipitation case 6 and intermediate reaction case 7, described one-level stirring coagulation case 2 is connected with outside waste water water tank,
The outlet of described intermediate reaction case 7 is connected with the water inlet of described MVR vaporizer 1, and described coagulation pretreatment device also wraps
Include dewaterer 8, the charging aperture of described dewaterer 8 respectively with the discharging opening of described one-level settling tank 3 and described two-stage precipitation case 6
Discharging opening be connected.
Described triple effect concentrated solution forced circulation crystallizer 23 include the first effect heating evaporation room 9, first imitate separation chamber 10, the
Separation chamber 12, triple effect heating evaporation room 13, triple effect separation chamber 14, final condenser are imitated in two effect heating evaporation rooms 11, second
15, final Crystallization Separation machine 16 and distillation water pot 17, the water inlet of described first effect heating evaporation room 9 evaporates with described MVR
The leakage fluid dram of device 1 is connected, the outlet of described first effect heating evaporation room 9 and the described first water inlet phase imitating separation chamber 10
Connecting, the outlet of described first effect separation chamber 10 is connected with the described second water inlet imitating heating evaporation room 11, and described the
The outlet of two effect heating evaporation rooms 11 is connected with the water inlet of described second effect separation chamber 12, described second effect separation chamber 12
Outlet be connected with the water inlet of described triple effect heating evaporation room 13, the outlet of described triple effect heating evaporation room 13
Being connected with the water inlet of described triple effect separation chamber 14, the discharging opening of described triple effect separation chamber 14 divides with described final crystallization
Disembark 16 charging aperture be connected, described first effect heating evaporation room 9 air inlet with outside saturated vapor source 18 be connected, institute
State the gas outlet of the first effect heating evaporation room 9, the gas outlet of described second effect heating evaporation room 11 and the heating of described triple effect
The gas outlet of vaporization chamber 13 air inlet with described final condenser 15 respectively is connected, the gas outlet of described final condenser 15
Connect outer exhaust duct group 22, described second effect heating evaporation room 11, described triple effect heating evaporation room 13 and described finally
Condenser 15 be provided with distilled water discharging mouth and respectively water inlet with described distillation water pot 17 be connected.
Described first effect separation chamber 10, described second effect separation chamber 12 and described triple effect separation chamber 14 are provided with dense
Liquid refluxing opening and venthole, the described first dope refluxing opening of effect separation chamber 10 and entering of described first effect heating evaporation room 9
The mouth of a river is connected, and the dope refluxing opening of described second effect separation chamber 12 is connected with the water inlet of described second effect heating evaporation room 11
Connecing, the dope refluxing opening of described triple effect separation chamber 14 is connected with the water inlet of described triple effect heating evaporation room 13, described
The venthole of the first effect separation chamber 10 is connected with the air inlet of described second effect heating evaporation room 11, described second effect separation chamber
The venthole of 12 is connected with the air inlet of described triple effect heating evaporation room 13, the venthole of described triple effect separation chamber 14 with
The air inlet of described final condenser 15 is connected.
Described desulfurizing waste water processing device also includes heat exchanger group 19 and condensate water pot 20, described condensate water pot 20
Water inlet is connected with the distilled water discharging mouth of described first effect heating evaporation room 9, the outlet of described condensate water pot 20 and institute
The condensed water water inlet stating heat exchanger group 19 is connected, the gas outlet of described condensate water pot 20 and described first effect heating evaporation
The air inlet of room 9 is connected, and the outlet of described distillation water pot 17 is connected with the distilled water water inlet of described heat exchanger group 19
Connecing, the distilled water outlet tank up to standard with outside 21 of described heat exchanger group 19 is connected, in described heat exchanger group 19
It is additionally provided with the strong brine floss hole of strong brine import and brine outlet, described strong brine import and described MVR vaporizer 1
Being connected, described brine outlet is connected with the strong brine recovery port of described MVR vaporizer 1.
A kind of desulfuration waste water treatment process realized by above-mentioned desulfurizing waste water processing device, it comprises the following steps:
A. desulfurization wastewater is carried out pretreatment:
A. desulfurization wastewater is pumped to described one-level stirring coagulation case 2, in described one-level stirring coagulation case 2, adds poly-third simultaneously
Acrylamide (PAM) also stirs, and makes polyacrylamide (PAM) become greatly with the float generation flocculation reaction in waste water thus conglomeration；
B. precipitate and separate, precipitate and separate are carried out in the waste water reaction mixture produced in step a being delivered to described one-level settling tank 3
After the supernatant that obtains deliver to described two grades of stirring coagulation casees 4, after separation, the solid sediment of gained is delivered to described dewaterer 8 and is entered
Row dehydration, then processes making outward transport after the solid sediment pack after dehydration to water content less than 60%；
C. add sodium carbonate and make it be sufficiently mixed with waste water in tank in described secondary response tank 4, add the main of sodium carbonate
Purpose is to remove the calcium ions and magnesium ions dissolved in waste water, by adding soda ash solution, generates calcium carbonate, magnesium carbonate precipitation, thus reaches
To sedimentation calcium ions and magnesium ions purpose；
Aluminium polychlorid (PAC) and polyacrylamide (PAM) is thrown in, further the most respectively in described two grades of stirring coagulation casees 4
Producing coagulating with the fine suspension in waste water and colloidal substance, by adsorption bridging effect, conglomeration becomes big and is prone to heavy
Form sediment；
E. precipitate and separate is carried out in the coagulant liquid in two-stage coagulation tank described in step d 5 is delivered to described two-stage precipitation case 6,
The solid such as calcium carbonate, magnesium carbonate and partial suspended solid precipitation are to the bottom of settling tank, and after separation, the supernatant of gained is delivered to
Described intermediate reaction case 7, after separation the solid sediment of gained be delivered to described dewaterer 8 carry out dehydration separate, after dehydration
After solid aqueous rate is less than 60%, outward transport processes；
F. in described intermediate reaction case 7, dilute hydrochloric acid is thrown in so that the pH value of the waste water in described intermediate reaction case 7 is reduced to
Between 5.5 and 6.5, eliminate the impact of remaining carbonate in waste water, prevent magnesium bicarbonate from converting during evaporation heating
Become carbonic acid magne-scale,
B. it is that the waste water between 5.5 and 6.5 is delivered to described MVR vaporizer 1, now waste water by the pH value of last for step A gained
Institute it is back to again after first passing through described heat exchanger group 19 and carrying out heat exchange with the distilled water flowing through described heat exchanger group 19
State MVR vaporizer 1 to decompose；Waste water is decomposed into on-condensible gas, distilled water and concentrated solution by described MVR vaporizer 1, wherein
On-condensible gas is emitted into outside by pipe group, and outer row to described MVR vaporizer 1 internal distillation water pot collected by distilled water；
C. the concentrated solution produced in step B is carried out triple effect forced circulation crystallization treatment:
In the concentrated solution that the most described MVR vaporizer 1 is produced is delivered to described heat exchanger group 19 and with from described condensed water
The condensed water discharged in tank 20 carries out heat exchange, and after completing, concentrated solution is transported to described triple effect concentrated solution forced circulation crystallizer
23；
H. carry out heating evaporation in completing that the concentrated solution of heat exchange is defeated and being sent to described first effect heating evaporation room 9 and decomposite secondary
Concentrated solution and water vapour, wherein water vapour is transported to described final condenser 15 and carries out condensation process, and secondary concentration liquid is defeated
Delivering to described first effect separation chamber 10 separate, in separation process, part secondary concentration liquid is back to described first effect heating
Heating evaporation, another part secondary concentration liquid and the effect steam decomposited is proceeded the most defeated in vaporization chamber 9
Deliver to described second effect heating evaporation room 11 carry out heating evaporation decomposite three concentrated solutions with two effect steam, wherein two imitate water
Steam is transported to described final condenser 15 and carries out condensation process, and three times concentrated solution is transported to described second effect separation chamber 12
Separating, in separation process, portion's concentrated solution in three times is back to described second effect heating evaporation room 11 and proceeds heating steaming
Send out；
I. three concentrated solutions of the another part in step h and two effect steam are transported to the heating steaming of described triple effect the most respectively
Carrying out heating evaporation in sending out room 13, thus decomposite four concentrated solutions and triple effect water vapour, wherein triple effect steam is transported to
Described final condenser 15 carries out condensation process, and four concentrated solutions are transported to described triple effect separation chamber 14 and carry out crystallization point
From, separation process is isolated crystal salt and four concentrated solutions of residue, wherein four concentrated solutions of residue are back to the described 3rd
Effect heating evaporation room 13 proceeds heating evaporation, the final steam in described triple effect separation chamber 14 be transported to described in
Whole condenser 15 carries out condensation process, and crystal salt carries out last water salt and separates in being sent to described final Crystallization Separation machine 16,
And finally sub-argument goes out final crystal salt and five concentrated solutions, wherein five concentrated solutions are back to described triple effect heating evaporation room
13 proceed heating evaporation, and final crystal salt is transported outward process.Described first heating evaporation room 9, described second heating are steamed
Send out the distilled water produced in room 11 and described 3rd heating evaporation room 13 and be transported to described distillation water pot 17 respectively, then through institute
State heat exchanger group 19 and be delivered to outside tank up to standard 21.
Step C iterative cycles is carried out, and to reach waste water is carried out separating treatment thoroughly, makes steam discharge reach simultaneously
Mark.
In this specific embodiment, described MVR vaporizer is mechanical steam recompression technology vaporizer.
The present invention is applicable to power plant desulfurization field of waste water treatment.
Claims (7)
1. a desulfurizing waste water processing device, it is characterised in that: it includes coagulation pretreatment device, MVR vaporizer (1) and three
Effect concentrated solution forced circulation crystallizer (23), described coagulation pretreatment device, described MVR vaporizer (1) and described triple effect are dense
Contracting liquid forced circulation crystallizer (23) is sequentially connected and connects, and described coagulation pretreatment device is connected with outside waste water water tank.
Desulfurizing waste water processing device the most according to claim 1, it is characterised in that: described coagulation pretreatment device includes depending on
Secondary be connected one-level stirring coagulation case (2), one-level settling tank (3), two grades stirring coagulation case (4), two-stage precipitation case (6) and
Intermediate reaction case (7), described one-level stirring coagulation case (2) is connected with outside waste water water tank, going out of described intermediate reaction case (7)
The mouth of a river is connected with the water inlet of described MVR vaporizer (1), and described coagulation pretreatment device also includes dewaterer (8), described de-
The charging aperture of water machine (8) respectively with discharging opening and the discharging opening phase of described two-stage precipitation case (6) of described one-level settling tank (3)
Connect.
Desulfurizing waste water processing device the most according to claim 2, it is characterised in that: described triple effect concentrated solution forced circulation is tied
Brilliant device (23) includes the first effect heating evaporation room (9), the first effect separation chamber (10), the second effect heating evaporation room (11), the second effect
Separation chamber (12), triple effect heating evaporation room (13), triple effect separation chamber (14), final condenser (15), final Crystallization Separation
Machine (16) and distillation water pot (17), the water inlet of described first effect heating evaporation room (9) and the row of described MVR vaporizer (1)
Liquid mouth is connected, and the outlet of described first effect heating evaporation room (9) is connected with the water inlet of described first effect separation chamber (10)
Connecing, the outlet of described first effect separation chamber (10) is connected with the water inlet of described second effect heating evaporation room (11), described
The outlet of the second effect heating evaporation room (11) is connected with the water inlet of described second effect separation chamber (12), described second effect point
It is connected with the water inlet of described triple effect heating evaporation room (13) from the outlet of room (12), described triple effect heating evaporation room
(13) outlet is connected with the water inlet of described triple effect separation chamber (14), the discharging opening of described triple effect separation chamber (14)
Being connected with the charging aperture of described final Crystallization Separation machine (16), the air inlet of described first effect heating evaporation room (9) is with outside
Saturated vapor source (18) is connected, the gas outlet of described first effect heating evaporation room (9), described second effect heating evaporation room (11)
Gas outlet and described triple effect heating evaporation room (13) gas outlet respectively with the air inlet of described final condenser (15)
Being connected, the gas outlet of described final condenser (15) connects outer exhaust duct group (22), described second effect heating evaporation room
(11), described triple effect heating evaporation room (13) and described final condenser (15) are provided with distilled water discharging mouth difference
It is connected with the water inlet of described distillation water pot (17).
Desulfurizing waste water processing device the most according to claim 3, it is characterised in that: described first effect separation chamber (10), institute
State the second effect separation chamber (12) and described triple effect separation chamber (14) is provided with dope refluxing opening and venthole, described
The dope refluxing opening of one effect separation chamber (10) is connected with the water inlet of described first effect heating evaporation room (9), described second effect
The dope refluxing opening of separation chamber (12) is connected with the water inlet of described second effect heating evaporation room (11), and described triple effect separates
The dope refluxing opening of room (14) is connected with the water inlet of described triple effect heating evaporation room (13), described first effect separation chamber
(10) venthole is connected with the air inlet of described second effect heating evaporation room (11), going out of described second effect separation chamber (12)
Pore is connected with the air inlet of described triple effect heating evaporation room (13), the venthole of described triple effect separation chamber (14) and institute
The air inlet stating final condenser (15) is connected.
Desulfurizing waste water processing device the most according to claim 4, it is characterised in that: described desulfurizing waste water processing device also wraps
Include heat exchanger group (19) and condensate water pot (20), the water inlet of described condensate water pot (20) and described first effect heating evaporation
The distilled water discharging mouth of room (9) is connected, the outlet of described condensate water pot (20) and the condensation of described heat exchanger group (19)
Water water inlet is connected, and the gas outlet of described condensate water pot (20) is connected with the air inlet of described first effect heating evaporation room (9)
Connecing, the outlet of described distillation water pot (17) is connected with the distilled water water inlet of described heat exchanger group (19), and described heat is handed over
Distilled water outlet tank up to standard with outside (21) of parallel operation group (19) is connected, and described heat exchanger group (19) also sets up
Strong brine import and brine outlet, described strong brine import is had to be connected with the strong brine floss hole of described MVR vaporizer (1)
Connecing, described brine outlet is connected with the strong brine recovery port of described MVR vaporizer (1).
6. the desulfuration waste water treatment process realized by the desulfurizing waste water processing device described in claim 5, its feature
It is: it comprises the following steps:
A. desulfurization wastewater is carried out pretreatment:
A. desulfurization wastewater is pumped to described one-level stirring coagulation case (2), adds in described one-level stirring coagulation case (2) simultaneously
Polyacrylamide also stirs, and makes polyacrylamide become greatly with the float generation flocculation reaction in waste water thus conglomeration；
B. precipitate and separate, precipitation point are carried out in the waste water reaction mixture produced in step a being delivered to described one-level settling tank (3)
The supernatant obtained after from delivers to described two grades of stirrings coagulation case (4), and after separation, the solid sediment of gained delivers to described dehydration
Machine (8) carries out being dehydrated to water content less than 60%, then processes making outward transport after the solid sediment pack after dehydration；
C. add sodium carbonate and make it be sufficiently mixed with waste water in tank in described two grades of stirrings coagulation case (4)；
Appropriate aluminium polychlorid and polyacrylamide is thrown in, further with useless the most respectively in described two grades of stirrings coagulation case (4)
Fine suspension and colloidal substance in water produce coagulating, and by adsorption bridging effect, conglomeration becomes big and is prone to precipitation；
E. carry out in the composite waste in described in step d two grades of stirrings coagulation case (4) being delivered to described two-stage precipitation case (6)
Precipitate and separate, after precipitate and separate, the supernatant of gained is delivered to described intermediate reaction case (7), the solid sediment of gained after separation
It is delivered to described dewaterer (8) carry out being dehydrated to moisture content and transporting outward less than 60% and after packed for the solid sediment after dehydration
Process；
F. in described intermediate reaction case (7), dilute hydrochloric acid is thrown in so that the pH value of the waste water in described intermediate reaction case (7) reduces
Between 5.5 to 6.5, eliminate the impact of remaining carbonate in waste water；
B., the waste water of last for step A gained is delivered to described MVR vaporizer (1), and waste water is decomposed by described MVR vaporizer (1)
For on-condensible gas, distilled water and concentrated solution, wherein on-condensible gas is emitted into outside by pipe group, and distilled water is collected to described
Outer row after MVR vaporizer (1) internal distillation water pot；
C. the concentrated solution produced in step B is carried out triple effect forced circulation crystallization treatment:
The concentrated solution that the most described MVR vaporizer (1) is produced be delivered in described heat exchanger group (19) and with from described cold
The condensed water discharged in solidifying water pot (20) carries out heat exchange, and after completing, concentrated solution is transported to described triple effect concentrated solution forced circulation
Crystallizer (23)；
H. carry out heating evaporation in completing that the concentrated solution of heat exchange is defeated and being sent to described first effect heating evaporation room (9) and decomposite two
Secondary concentrated solution and water vapour, wherein water vapour is transported to described final condenser (15) and carries out condensation process, secondary concentration liquid
Being transported to described first effect separation chamber (10) separate, in separation process, part secondary concentration liquid is back to described first
Proceeding heating evaporation in effect heating evaporation room (9), another part secondary concentration liquid and the effect steam that decomposites are then
Be transported to respectively described second effect heating evaporation room (11) carry out heating evaporation decomposite three concentrated solutions with two imitate steam,
Wherein two effect water vapour are transported to described final condenser (15) and carry out condensation process, and three concentrated solutions are transported to described the
Two effects separation chamber (12) separate, and in separation process, portion's concentrated solution in three times is back to described second effect heating evaporation room
(11) heating evaporation is proceeded；
I. three concentrated solutions of the another part in step h and two effect steam are transported to the heating steaming of described triple effect the most respectively
Carrying out heating evaporation in sending out room (13), thus decomposite four concentrated solutions and triple effect water vapour, wherein triple effect steam is carried
Carrying out condensation process to described final condenser (15), four concentrated solutions are transported to described triple effect separation chamber (14) and tie
Brilliant separation, isolates crystal salt and four concentrated solutions of residue in separation process, wherein four concentrated solutions of residue are back to described
Triple effect heating evaporation room (13) proceeds heating evaporation, and the final steam in described triple effect separation chamber (14) is carried
Carry out condensation process to described final condenser (15), and crystal salt is carried out in being sent to described final Crystallization Separation machine (16)
Rear water salt separates, and final sub-argument goes out final crystal salt and five concentrated solutions, and wherein five concentrated solutions are back to the described 3rd
Effect heating evaporation room (13) proceeds heating evaporation, and final crystal salt is transported outward process.
Desulfuration waste water treatment process the most according to claim 6, it is characterised in that: in step C, described first effect heating
The distilled water produced in vaporization chamber (9), described second effect heating evaporation room (11) and described triple effect heating evaporation room (13)
It is transported to described distillation water pot (17) respectively, then is delivered to outside tank up to standard (21) through described heat exchanger group (19).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108275822A (en) * | 2018-03-20 | 2018-07-13 | 山东奥能电力科技有限公司 | A kind of dense salt waste water atomization concentration cycles crystallization Zero discharging system and technique |
| CN108395041A (en) * | 2018-03-01 | 2018-08-14 | 中国电建集团透平科技有限公司 | A kind of system for handling desulfurization wastewater |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090294377A1 (en) * | 2008-05-29 | 2009-12-03 | Hpd, Llc | Method for Removing Dissolved Solids from Aqueous Waste Streams |
| US20100163471A1 (en) * | 2008-12-30 | 2010-07-01 | Irving Elyanow | Water desalination plant and system for the production of pure water and salt |
| CN102060408A (en) * | 2010-12-07 | 2011-05-18 | 华电水处理技术工程有限公司 | Wastewater evaporating process and device system |
| CN102070272A (en) * | 2010-12-07 | 2011-05-25 | 华电水处理技术工程有限公司 | Wastewater evaporation concentration process and device system |
| CN104208902A (en) * | 2014-09-28 | 2014-12-17 | 湖北吉星化工集团有限责任公司 | Triple-effect evaporation and crystallization production process and device |
| CN205204972U (en) * | 2015-10-16 | 2016-05-04 | 上海晶宇环境工程股份有限公司 | Coal fired power plant desulfurization waste water zero release treatment process's isolated plant |
| CN105692998A (en) * | 2016-03-08 | 2016-06-22 | 上海朴是环境科技有限公司 | Desulfurized waste water zero-emission system and technology adopting redissolution for salt and nitrate supplementation and realizing salt separation for recycling |
| CN205676308U (en) * | 2016-06-24 | 2016-11-09 | 珠海昊森万荣水处理科技有限公司 | Desulfurizing waste water processing device |
-
2016
- 2016-06-24 CN CN201610467661.4A patent/CN106082514A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090294377A1 (en) * | 2008-05-29 | 2009-12-03 | Hpd, Llc | Method for Removing Dissolved Solids from Aqueous Waste Streams |
| US20100163471A1 (en) * | 2008-12-30 | 2010-07-01 | Irving Elyanow | Water desalination plant and system for the production of pure water and salt |
| CN102060408A (en) * | 2010-12-07 | 2011-05-18 | 华电水处理技术工程有限公司 | Wastewater evaporating process and device system |
| CN102070272A (en) * | 2010-12-07 | 2011-05-25 | 华电水处理技术工程有限公司 | Wastewater evaporation concentration process and device system |
| CN104208902A (en) * | 2014-09-28 | 2014-12-17 | 湖北吉星化工集团有限责任公司 | Triple-effect evaporation and crystallization production process and device |
| CN205204972U (en) * | 2015-10-16 | 2016-05-04 | 上海晶宇环境工程股份有限公司 | Coal fired power plant desulfurization waste water zero release treatment process's isolated plant |
| CN105692998A (en) * | 2016-03-08 | 2016-06-22 | 上海朴是环境科技有限公司 | Desulfurized waste water zero-emission system and technology adopting redissolution for salt and nitrate supplementation and realizing salt separation for recycling |
| CN205676308U (en) * | 2016-06-24 | 2016-11-09 | 珠海昊森万荣水处理科技有限公司 | Desulfurizing waste water processing device |
Non-Patent Citations (1)
| Title |
|---|
| 王淑勤等: "《电厂化学技术》", 31 March 2007, 北京：中国电力出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108395041A (en) * | 2018-03-01 | 2018-08-14 | 中国电建集团透平科技有限公司 | A kind of system for handling desulfurization wastewater |
| CN108275822A (en) * | 2018-03-20 | 2018-07-13 | 山东奥能电力科技有限公司 | A kind of dense salt waste water atomization concentration cycles crystallization Zero discharging system and technique |
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