CN206858347U - A kind of device of desulfurization wastewater sub-prime crystallization treatment - Google Patents
A kind of device of desulfurization wastewater sub-prime crystallization treatment Download PDFInfo
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- CN206858347U CN206858347U CN201720510730.5U CN201720510730U CN206858347U CN 206858347 U CN206858347 U CN 206858347U CN 201720510730 U CN201720510730 U CN 201720510730U CN 206858347 U CN206858347 U CN 206858347U
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Abstract
It the utility model is related to a kind of device of desulfurization wastewater sub-prime crystallization treatment, desulfurization wastewater can be softened into preconditioning technique, membrane separation technique and crystallization technique using described device effectively to combine, softening pretreatment first is carried out to desulfurization wastewater, reduces the hardness of desulfurization wastewater；A point salt treatment, concentration are carried out to softening pretreated desulfurization wastewater using membrane separation technique again, sodium sulphate therein and sodium chloride are separated；The sodium sulphate finally reclaimed using crystallisation by cooling in waste water prepares the sal glauberi crystal of purity >=98%, and the sodium chloride crystal for preparing purity >=94% is handled using evaporative crystallization, realizes that desulfurization wastewater no pollution discharges.It is high that the utility model solves the direct evaporation energy consumption of desulfurization wastewater, the easy fouling of equipment and evaporation gained mixed salt are difficult to the technical barrier recycled, it is cost-effective, the maximum recycling of desulfurization wastewater is realized, truly realizes comprehensively recyling for desulfurization wastewater.
Description
Technical field
It the utility model is related to sewage treatment area, and in particular to a kind of advanced treating of desulfurization wastewater realizes zero-emission
Method and apparatus.
Background technology
The enterprise of China's supply of electric power at present is generally carried out at desulfurization using Wet Limestone-desulfurization of gypsum technique to flue gas
Reason, because its have the advantages that desulfuration efficiency it is high, using coal is wide, gypsum is used widely using technology maturation.Wet desulphurization
During technique desulfurization, slurries iterative cycles utilize in desulfuration absorbing tower, and soluble salt slurries constantly concentrate in tower, to ensure desulfurization performance
With chloride equilibrium in maintenance system, it is necessary to be continuously replenished, update slurries, the underflow liquid in absorption tower separates through hydrocyclone
Supernatant afterwards, i.e. desulfurization wastewater.Desulfurization wastewater must be discharged periodically from system.
The general water of desulfurization wastewater is little, in faintly acid, but containing substantial amounts of suspension, sulfate, chloride, hardness from
Son and micro heavy, directly discharge have serious harm to environment, it is necessary to are strictly handled.Traditional " three headers " work
Skill be by desulfurization is useless carry out preliminary sedimentation processing after, then it is neutralized, flocculated and precipitation process, remove suspension in waste water and
The materials such as heavy metal, the handling process water outlet salt content is still higher, is often directly used in power plant's punching ash in the past, but with environmental requirement
Continuous improvement, desulfurization wastewater advanced treatment and reclamation, realize wastewater zero discharge, be increasingly becoming the development trend of industry.
At present, evaporative crystallization technique is the prevailing technology for realizing desulfurization wastewater zero discharge treatment, but direct evaporated water
Larger, energy consumption and investment cost are higher, and the easy fouling of evaporation equipment, and salt caused by evaporative crystallization is sodium chloride and sodium sulphate
Mixed salt, it is difficult to recycle.
Utility model content
In order to solve the technical barrier that evaporation energy consumption height, the easy fouling of equipment, and evaporation gained mixed salt are difficult to recycle,
The utility model provides a kind of device of desulfurization wastewater sub-prime crystallization treatment, including
Soften pretreatment system,
Ultra-filtration and separation system,
Sludge treating system,
Sodium ion melded system,
Nanofiltration divides salt system,
Counter-infiltration system
And crystal system,
Desulfurization wastewater regulating reservoir is unidirectionally connected with the softening pretreatment system,
The softening pretreatment system is connected with the ultra-filtration and separation one-way system,
The ultra-filtration and separation system is unidirectionally connected with the sodium ion melded system, the ultra-filtration and separation system and the dirt
Mud treatment system unidirectionally connects,
The sludge treating system is unidirectionally connected with desulfurization wastewater regulating reservoir,
The sodium ion melded system is unidirectionally connected with the nanofiltration point salt system,
The nanofiltration point salt system is unidirectionally connected with the counter-infiltration system,
The counter-infiltration system is unidirectionally connected with the crystal system.
It is described it is unidirectional be connected as from previous system to the latter system can not reverse connection, as described above, desulfurization wastewater
Regulating reservoir is unidirectionally connected with the softening pretreatment system, refers to unidirectionally can not from desulfurization wastewater regulating reservoir to softening pretreatment
Reverse connection.
The device of desulfurization wastewater sub-prime crystallization treatment as described above, the softening pretreatment system include unidirectionally connecting successively
The first reactive tank and the second reactive tank connect, it is preferable that be equipped with stirring in first reactive tank and second reactive tank
Device.
Desulfurization wastewater after desulfurization wastewater regulating reservoir homogeneous, into the first reactive tank, according to coming alkalinity of water and hardness
Content, quantitative sodium hydroxide solution is added in the first reactive tank, coarse adjustment is carried out to pH value, control ph is anti-in 10-11, first
Answer and agitating device is provided with groove, sodium hydroxide solution and the abundant haptoreaction of desulfurization wastewater are made by stirring, made in desulfurization wastewater
Magnesium ion and heavy metal ion generation hydroxide precipitation, and make through the first reactive tank handle desulfurization wastewater with coagulation state
Into the second reactive tank.Continue to add sodium hydroxide and sodium carbonate liquor in the second reactive tank, accurate adjustment is carried out to pH, controls pH
Value is again provided with agitating device in 11 or so, second reactive tanks so that reaction is more complete.Make the calcium ion in desulfurization wastewater
With the abundant haptoreaction of carbanion, precipitation of calcium carbonate is generated, and desulfurization wastewater is entered ultrafiltration system with coagulation state
Concentrate water tank.
The device of desulfurization wastewater sub-prime crystallization treatment as described above, what the ultra-filtration and separation system included being sequentially connected surpasses
Filter influent pump, hyperfiltration membrane assembly and intermediate water tank, it is preferable that the hyperfiltration membrane assembly is tubular ultrafiltration membrane module.
Desulfurization wastewater in concentration water tank enters hyperfiltration membrane assembly by ultrafiltration intake pump, and cross-flow is selected in ultrafiltration system design
The form of filtering, hyperfiltration membrane assembly water outlet are divided into two parts：100mg/L is not higher than through the production water hardness of milipore filter, in inflow
Between water tank, the concentrate for a large amount of sediments of carrying being rejected by then returns to concentration water tank and further circulates concentration.Milipore filter group
Part is resistant to pollution tubular ultrafiltration membrane module, and molecular cut off is the Dalton of 10-25 ten thousand, operating pressure 1-6bar, tubular membrane
Flow diameter is 6,8 or 12mm.
The device of desulfurization wastewater sub-prime crystallization treatment as described above, the sludge treating system include the dirt being sequentially connected
Mud thickener and filter press.
The ultrafiltration concentrated water for carrying a large amount of sediments returns to concentration water tank, and concentration water tank periodically discharges height according to according to solution concentration
Sludge can be dehydrated by the mud mixture of concentration to sludge concentration tank, mud treatment system by filter press, form it into dirt
The mud cake of mud concentration 60%, squeeze water return to desulfurization wastewater regulating reservoir.
The device of desulfurization wastewater sub-prime crystallization treatment as described above, the sodium ion melded system include what is be sequentially connected
Intake pump and Na-ion exchanger.
The water outlet of intermediate water tank enters Na-ion exchanger by Na-ion exchanger intake pump, further removes and carrys out hydraulic
Degree, Na-ion exchanger, which goes out the water hardness, can be down to below 3mg/L, and condition is created for the concentration of subsequent film high power.
The device of desulfurization wastewater sub-prime crystallization treatment as described above, it is preferable that the nanofiltration divides salt system to be dish tubular type
Nanofiltration divides salt system, and the dish tubular type nanofiltration point salt system includes intake pump, accurate filter, the high-pressure plunger being sequentially connected
Pump, booster pump and dish tubular nanofiltration membrane component.
Na-ion exchanger water outlet enters accurate filter by dish tubular type nanofiltration intake pump, and accurate filter filtering accuracy is
10 μm, can remove small impurity in water, provided for high-pressure plunger pump with film post together with favourable protective barrier.Due to high-pressure pump
The flow velocity and underfed of water outlet to all membrane modules directly to supply water, so booster pump is set before membrane module, booster pump
The pump advancing water of suction, the concentrate that a part has flowed through membrane module, so, supercharging are also included in addition to high-pressure plunger pump feeds water
The setting of pump both ensure that there were enough flow and flow rates on film surface, effectively prevent the dirt of the film caused by flow velocity is too low
Dye, has been significantly increased the recycle-water rate of system again.Dish tubular nanofiltration membrane piece to the removal efficiency of sulfate radical can up to more than 99%,
To the even negative retention of sodium chloride, dish tubular type nanofiltration system permeate is set to be essentially sodium chloride solution, concentrate is substantially sulphur
Acid sodium solution, ensure that later crystallization divides the purity of salt.
The device of desulfurization wastewater sub-prime crystallization treatment as described above, the counter-infiltration system include the first counter-infiltration system
With the second counter-infiltration system, it is preferable that first counter-infiltration system and second counter-infiltration system are two identical and phases
Mutually independent disc tube reverse osmosis (dt-ro) system, the nanofiltration point salt system are unidirectionally connected with the disc tube reverse osmosis (dt-ro) system respectively,
Further, the disc tube reverse osmosis (dt-ro) system include be sequentially connected intake pump, accurate filter, high-pressure plunger pump, supercharging
Pump and disc tube reverse osmosis (dt-ro) membrane module.
The concentrate or permeate of nanofiltration system enter accurate filter by each supporting intake pump respectively, go to remove water
In small impurity, subsequently into the high-pressure pump of system support.Booster pump is set between high-pressure pump and membrane module, and booster pump enters
Water also includes the concentrate that a part has flowed through membrane module in addition to high-pressure plunger pump feeds water, to provide foot to all membrane modules
Enough flow of inlet water and flow velocity.
What disc tube reverse osmosis (dt-ro) system was selected is reverse osmosis membrane, has higher rejection to sodium chloride and sodium sulphate,
It is generally not less than 97% to the rejection of sodium chloride and sodium sulphate, and disc tube reverse osmosis (dt-ro) system can be entered to nanofiltration system water outlet
The concentration minimizing processing of row high power, production water meet that recycle-water requirement is reused.The protrusion of disc tube reverse osmosis (dt-ro) membrane module
Feature is that contamination resistance is strong and stress levels are high, and 10000mg/L situation can be not higher than in water COD (COD)
Under, still stable operation, stress levels are high, can carry out high power concentration and minimizing to water according to water water quality and processing requirement,
Sodium chloride solution can be concentrated into 100000mg/L by highest, metabisulfite solution can be concentrated into 150000mg/L.
The device of desulfurization wastewater sub-prime crystallization treatment as described above, the crystal system include separate freezing knot
Crystallographic system is united and evaporation and crystallization system, first counter-infiltration system are unidirectionally connected with the freezing and crystallizing system, and described second is anti-
Osmosis system is unidirectionally connected with the evaporation and crystallization system, and further, the freezing and crystallizing system is cold including being sequentially connected
Freeze crystallization kettle and centrifugal dehydrator, the evaporation and crystallization system includes the evaporative crystallization kettle and centrifugal dehydrator being sequentially connected.
It is dehydrated after the chilled crystallization kettle processing of the concentrated metabisulfite solution of counter-infiltration system, then through centrifugal dehydrator,
The sal glauberi of purity more than 98% is obtained, denitration liquid returns to the water inlet end of nanofiltration system, reprocessed.Through counter-infiltration
The concentrated sodium chloride solution of system is handled by crystallizing evaporator, and steam condensate (SC) collects reuse, and the evaporation of discharge system is dense
Liquid can obtain the industrial wet salt of purity >=94% after centrifugal dehydrator is handled, and centrifuge mother liquor returns to sodium chloride crystallizing evaporator
Further processing.
The utility model also provides a kind of method of desulfurization wastewater sub-prime crystallization treatment, comprises the following steps：
(1) by desulfurization wastewater homogenization；
(2) by sodium hydroxide solution and mass concentration that mass concentration is 20%-40% be 20%-30% sodium carbonate it is molten
Liquid is successively added in the desulfurization wastewater of homogenization, adjusts the pH value of solution in 10-11, desulfurization wastewater is carried out to soften pre- place
Reason, make in desulfurization wastewater most calcium ion and magnesium ion and heavy metal ion in the form of hydroxide and carbonated
Precipitation；
(3) ultra-filtration and separation will be carried out by the desulfurization wastewater for softening pretreatment, filters off precipitation, obtain passing through water；
(4) sofening treatment again is carried out through water using what Na-ion exchanger obtained to ultra-filtration and separation, further removed
Through the calcium ion and magnesium ion in water, the hardness of water outlet is obtained in below 3mg/L；
(5) divide water outlet progress nanofiltration to salt treatment using nano-filtration membrane equipment, separate sodium chloride and sodium sulphate in solution, obtain
To sodium chloride solution and metabisulfite solution；
(6) concentration is carried out to sodium chloride solution and metabisulfite solution using reverse osmosis membrane equipment, quality can be obtained
The sodium chloride solution that the metabisulfite solution and mass concentration that concentration is 15% are 10%；
(7) metabisulfite solution for crossing concentration carries out Freeze crystallization, obtains sal glauberi crystal and denitration
Liquid；
(8) sodium chloride solution for crossing concentration is evaporated crystallization treatment, obtains sodium chloride crystal.
Preferably, for ultra-filtration and separation by the way of cross-flow filtration, sediment is trapped within concentrated water side in step (3), passes through
The water hardness is can be controlled in not higher than 100mg/L.
Chemical dosing is combined with ultrafiltration, compared with tradition softens gravitational settling method, is saved and is built needed for sedimentation basin
Civil engineering costs, and flocculant need not be added sediment is formed big alumen ustum and sediment totally can thoroughly be removed, gone out
Water turbidity is not higher than 1NTU, is laid a good foundation for the stable operation of subsequent nano-filtration membranous system.
To occur the tendency that hardness ions is enriched with fouling when avoiding follow-up membranous system from concentrating water high power, according to concentration times
Number high request, ultra-filtration and separation system is further handled through water from sodium ion demineralizer, hardness is removed, can will go out hydraulic
Degree is down to below 3mg/L.
Preferably, dehydration is carried out in step (3) to the precipitation obtained by desulfurization wastewater ultra-filtration and separation and mud cake, the mud cake is made
Sludge quality concentration be more than 60%, dehydration gained liquid return to step (2) reprocessed.
Preferably, nano-filtration membrane equipment is dish tubular nanofiltration membrane equipment in step (5), removing of the selected NF membrane to sulfate radical
Rate even bears retention up to more than 99%, to sodium chloride, dish tubular type nanofiltration system permeate is essentially sodium chloride solution, dense
Contracting liquid is substantially metabisulfite solution, ensures that later crystallization divides the purity of salt, in addition, dish tubular membrane component in antifouling property and
It is substantially improved in terms of stress levels compared with rolled membrane module, and then ensure that the stability of system operation and water is concentrated
The maximization of separation.
Preferably, concentration, dish tubular type nanofiltration are carried out to desulfurization wastewater using disc tube reverse osmosis (dt-ro) system in step (6)
Water outlet is divided into concentrate and permeate two parts, and wherein concentrate is the solution based on sodium sulphate, and permeate is with sodium chloride
Based on solution, to improve solution concentration, reduce the processing load of follow-up freezing and evaporative crystallization unit, reduce whole system
Operating cost, use can overcome the disc tube reverse osmosis (dt-ro) membranous system compared with hyperosmosis to carry out at high power concentration minimizing for the two
Reason, the production water recoverable of disc tube reverse osmosis (dt-ro) membranous system.
Preferably, the denitration liquid return to step (5) obtained by step (7) described freezing and crystallizing is handled again, by denitration
Liquid returns to (5) and handled again.
The beneficial effects of the utility model are：A kind of dress of desulfurization wastewater sub-prime crystallization treatment provided by the utility model
Put, desulfurization wastewater can be softened into preconditioning technique, membrane separation technique and crystallization technique using described device effectively combines, first
Softening pretreatment is carried out to desulfurization wastewater, reduces the hardness of desulfurization wastewater；It is pretreated to softening using membrane separation technique again
Desulfurization wastewater carries out a point salt treatment, concentration, and sodium sulphate therein and sodium chloride are separated；It is last to utilize cooling knot simultaneously
Sodium sulphate in crystalline substance recovery waste water prepares the sal glauberi crystal that purity reaches more than 98%, is handled and made using evaporative crystallization
For the sodium chloride crystal that purity reaches more than 94% is gone out, realize that desulfurization wastewater no pollution discharges.The utility model solves desulfurization
The direct evaporation energy consumption of waste water is high, the easy fouling of equipment, and evaporates the technical barrier that gained mixed salt is difficult to recycle, and saves into
This, realizes the maximum recycling of desulfurization wastewater, truly realizes comprehensively recyling for desulfurization wastewater.
Brief description of the drawings
, below will be to embodiment in order to illustrate more clearly of the utility model embodiment or technical scheme of the prior art
Or the required accompanying drawing used is briefly described in description of the prior art, it should be apparent that, drawings in the following description are only
It is some embodiments of the utility model, for those of ordinary skill in the art, is not paying the premise of creative work
Under, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is FGD Wastewater Treatment Process figure；
Fig. 2 is desulfurizing waste water processing device figure.
The reactive tanks of 1- first in figure；2-1# agitators；The reactive tanks of 3- second；4-2# agitators；5- concentrates water tank；6- ultrafiltration
Intake pump；7- hyperfiltration membrane assemblies；8- intermediate water tanks；9- Na-ion exchanger intake pumps；10- Na-ion exchangers；11- sludge is dense
Contracting groove；12- filter presses；13-1# intake pumps；14-1# accurate filters；15-1# high-pressure plunger pumps；16-1# booster pumps；17- receives
Filter membrane component；18-2# intake pumps；19-2# accurate filters；20-2# high-pressure plunger pumps；21-2# booster pumps；22-1# counter-infiltrations
Membrane module；23-3# intake pumps；24-3# accurate filters；25-3# high-pressure plunger pumps；26-3# booster pumps；27-2# reverse osmosis membranes
Component；28- freezing and crystallizing kettles；29-1# centrifugal dehydrators；30- crystallizing evaporators；31-2# centrifugal dehydrators.
Embodiment
, below will be to technology of the present utility model to make the purpose of this utility model, technical scheme and advantage clearer
Scheme is described in detail.Obviously, described embodiment is only the utility model part of the embodiment, rather than all
Embodiment.Based on the embodiment in the utility model, those of ordinary skill in the art are not before creative work is made
Resulting all other embodiment is put, belongs to the scope that the utility model is protected.
The utility model provides a kind of device of desulfurization wastewater sub-prime crystallization treatment, and described device is soft including being sequentially connected with
Change pretreatment system, ultra-filtration and separation system, sludge treating system, sodium ion melded system, nanofiltration divide salt system, counter-infiltration system
And crystal system；Softening pretreatment system includes the 1# reactive tanks being sequentially connected, 2# reactive tanks 3 and concentration water tank 5, wherein 1#
There are the 1# agitators 2 for stirring in reactive tank, there are 2# agitators 4 in 2# reactive tanks 3；Ultra-filtration and separation system includes being sequentially connected
Ultrafiltration intake pump 6, hyperfiltration membrane assembly 7 and intermediate water tank 8；Sludge treating system includes the He of sludge concentration tank 11 being sequentially connected
Filter press 12；Sodium ion melded system includes the Na-ion exchanger intake pump 9 and Na-ion exchanger 10 being sequentially connected；Nanofiltration
1# intake pumps 13 that point salt system includes being sequentially connected, 1# accurate filters 14,1# high-pressure plunger pumps 15,1# booster pumps 16 and receive
Filter membrane component 17；Counter-infiltration system includes two identical and mutually independent counter-infiltration systems, wherein the first counter-infiltration system bag
Include the 2# intake pumps 18 being sequentially connected, 2# accurate filters 19,2# high-pressure plunger pumps 20,2# booster pumps 21 and 1# reverse osmosis membrane groups
Part 22, the second counter-infiltration system include 3# intake pumps 23,3# accurate filters 24,3# high-pressure plunger pumps 25, the 3# being sequentially connected
Booster pump 26 and 2# reverse osmosis membrane assemblies 27；Crystal system includes freezing and crystallizing system and evaporation and crystallization system, the freezing knot
Crystallographic system system includes the freezing and crystallizing kettle 28 and 1# centrifugal dehydrators 29 being sequentially connected, and the evaporation and crystallization system includes being sequentially connected
Evaporative crystallization kettle 30 and 2# centrifugal dehydrators 31.
A kind of method for desulfurization wastewater sub-prime crystallization treatment that the utility model also provides, its technological process are：Desulfurization is given up
Water softening pretreatment, ultrafiltration, sodium ion exchange processing, nanofiltration divide salt treatment, reverse-osmosis treated, freezing and crystallizing and evaporative crystallization.
Embodiment 1
Certain desulfurization wastewater project, handle water 22t/h, influent quality：pH：7.16, total dissolved solid (TDS)：
49750mg/L, Cl-：20821.8mg/L SO4 2-：3534.3mg/L Mg2+：6220mg/L, Ca2+：1933mg/L, HCO3 -：
60.556mg/L, COD (COD)：944.68mg/L.
Processing requirement：Water outlet reaches Controlling Auxiliaries in Power Plants cooling water quality standard：pH:6-9, total dissolved solid (TDS)≤1000mg/
L, Cl-：≤ 250mg/L, SO4 2-：≤ 250mg/L, total hardness is (with CaCO3Meter)≤450mg/L, COD (COD)≤
50mg/L, effluent reuse divide salt, and waste water realizes zero discharge treatment.
From technique：
Softening pretreatment → ultrafiltration → Na-ion exchanger → dish tubular type nanofiltration divides salt → disc tube reverse osmosis (dt-ro) → freezing knot
Brilliant and evaporative crystallization.
After the adjusted pond preliminary sedimentation processing of desulfurization wastewater, into 1# reactive tanks 1, adding mass concentration in 1# reactive tanks 1 is
30% sodium hydroxide solution 1.63t/h, make its pH value in 10-11, by the stirring of 1# agitators 2 make sodium hydroxide solution with it is de-
The abundant haptoreaction of sulphur waste water, hydraulic detention time 20 minutes, subsequently into 2# reactive tanks 3, continue to add matter in 2# reactive tanks 3
The sodium hydroxide solution that concentration is 30% is measured, control ph is 11 or so, while it is molten to add the sodium carbonate that mass concentration is 25%
Liquid 0.46t/h, stirred by 2# agitators 4, control hydraulic detention time 20 minutes, make medicament and the abundant haptoreaction of waste water,
And it is set to enter the concentration water tank 5 of ultrafiltration system with coagulation state.
Ultrafiltration system is designed as cross-flow filtration, and ultrafiltration intake pump 6 supplies water to hyperfiltration membrane assembly 7, by taking for milipore filter retention
Concentrate with a large amount of sediments returns to concentration water tank 5 and further circulation concentration is mixed with water, and the concentration sludge concentration of water tank 5 reaches
During to 3-4%, sludge condensation liquid is discharged to sludge concentration tank 11,11 hydraulic detention time of sludge concentration tank 12 hours, high power is dense
The sludge condensation liquid of contracting carries out press dewatering, caused mud cake is about with plate and frame filter press 12 from concentration trench bottom discharge to it
1.06t/h, sludge content is not less than 60%, pressure a small amount of in a small amount of supernatant and plate and frame filter press 12 in sludge concentration tank 11
Water is squeezed, then returns to 1# reactive tanks 1 and further handles.
The permeate hardness of ultrafiltration system is less than 100mg/L, and turbidity enters intermediate water tank 8 less than 1NTU, to intermediate water tank 8
The technical-grade hydrochloric acid that mass concentration is 30-37% is added, it is 7 or so to control its pH, is then entered by Na-ion exchanger intake pump 9
Enter Na-ion exchanger 10, further remove hardness, Na-ion exchanger 10, which goes out the water hardness, can be down to below 3mg/L.
Through except the water pre-processed firmly is through the entrance 1# of 1# intake pumps 13 accurate filters 14, the filtering accuracy of 1# accurate filters 14
For 10 μm, after removing impurity small in water removal, then after 1# high-pressure pumps 15 and 1# booster pumps 16 boost, into dish tubular nanofiltration membrane
Component, dish tubular nanofiltration membrane component select normal pressure level 75bar film posts, and diaphragm uses the extraordinary nanofiltration dedicated for solventing-out
Film.Dish tubular type nanofiltration system recycle-water rate is 90%, by chlorion and sulfate ion can efficiently separate, dish pipe
Formula nanofiltration system concentrate sulfate ion content can be concentrated into 35000mg/L, and permeate chloride ion content is 23000mg/L.
The concentrate and permeate of nanofiltration system are respectively adopted the first and second disc tube reverse osmosis (dt-ro) systems and concentrated again
Processing.Two sets of disc tube reverse osmosis (dt-ro) systems use 90bar hiigh pressure stage dish tubular membrane posts, and diaphragm is used to chlorion and sulfuric acid
The high reverse osmosis membrane of radical ion rejection.First disc tube reverse osmosis (dt-ro) system recycle-water rate is 65.5%, sulfate radical after concentration
Ion concentration 101449.3mg/L, the second disc tube reverse osmosis (dt-ro) system recycle-water rate are 55%, chloride ion content after concentration
51000mg/L.The permeate of two sets of counter-infiltration systems meets reuse requirement, recycling.
After the chilled crystallization kettle 28 of concentrate and 1# centrifugal dehydrators 29 processing of first disc tube reverse osmosis (dt-ro) system, obtain
The sal glauberi (saltcake) of purity >=98%, denitration liquid return to dish tubular type nanofiltration system water inlet end, reprocessed.Second dish
The concentrate of tubular type counter-infiltration system obtains the chlorine of purity >=95% after crystallizing evaporator 30 and 2# centrifugal dehydrators 31 are handled
Change sodium crystal, steam condensate (SC) collects reuse.
Embodiment 2
Certain desulfurization wastewater project, handle water 36t/h, influent quality：pH：7.24, total dissolved solid (TDS)：
35534.6mg/L Cl-：15000mg/L, SO4 2-：6000mg/L, Mg2+：600mg/L, Ca2+：2000mg/L, HCO3 -：65mg/
L, COD (COD)：95mg/L.
Processing requirement：Water outlet reaches circulating cooling water of power plant standard：pH:6-9, total dissolved solid (TDS)≤1000mg/
L, Cl-：≤ 250mg/L, SO4 2-：≤ 250mg/L, total hardness is (with CaCO3Meter)≤450mg/L, COD (COD)≤
50mg/L, effluent reuse divide salt, and waste water realizes zero discharge treatment.
From technique：
Softening pretreatment → ultrafiltration → Na-ion exchanger → nanofiltration divides salt → counter-infiltration → freezing and crystallizing and evaporative crystallization.
After the adjusted pond preliminary sedimentation processing of desulfurization wastewater, into 1# reactive tanks 1, adding mass concentration in 1# reactive tanks 1 is
20% sodium hydroxide solution 0.40t/h, make its pH value in 10-11, by the stirring of 1# agitators 2 make sodium hydroxide solution with it is de-
The abundant haptoreaction of sulphur waste water, hydraulic detention time 20 minutes, subsequently into 2# reactive tanks 3, continue to add matter in 2# reactive tanks 3
The sodium hydroxide solution that concentration is 20% is measured, control ph is 11 or so, while it is molten to add the sodium carbonate that mass concentration is 20%
Liquid 1.06t/h, stirred by 2# agitators 4, control hydraulic detention time 20 minutes, make medicament and the abundant haptoreaction of waste water,
And it is set to enter the concentration water tank 5 of ultrafiltration system with coagulation state.
Ultrafiltration system is designed as cross-flow filtration, and ultrafiltration intake pump 6 supplies water to hyperfiltration membrane assembly 7, by taking for milipore filter retention
Concentrate with a large amount of sediments returns to concentration water tank 5 and further circulation concentration is mixed with water, and the concentration sludge concentration of water tank 5 reaches
During to 3-4%, sludge condensation liquid is discharged to sludge concentration tank 11,11 hydraulic detention time of sludge concentration tank 12 hours, high power is dense
The sludge condensation liquid of contracting carries out press dewatering, caused mud cake is about with plate and frame filter press 12 from concentration trench bottom discharge to it
0.64t/h, sludge content is not less than 60%, pressure a small amount of in a small amount of supernatant and plate and frame filter press 12 in sludge concentration tank 11
Water is squeezed, then returns to 1# reactive tanks 1 and further handles.
The permeate hardness of ultrafiltration system is less than 100mg/L, and turbidity enters intermediate water tank 8 less than 1NTU, to intermediate water tank 8
The technical-grade hydrochloric acid that mass concentration is 30-37% is added, it is 7 or so to control its pH, is then entered by Na-ion exchanger intake pump 9
Enter Na-ion exchanger 10, further remove hardness, Na-ion exchanger 10, which goes out the water hardness, can be down to below 3mg/L.
Through except the water pre-processed firmly is through the entrance 1# of nanofiltration 1# intake pumps 13 accurate filters 14,1# accurate filters 14 filter
Precision is 10 μm, after removing impurity small in water removal, then after 1# high-pressure pumps 15 and 1# booster pumps 16 boost, into NF membrane group
Part 17, nanofiltration membrane component 17 select normal pressure level 75bar film posts, and diaphragm uses the extraordinary NF membrane dedicated for solventing-out.Receive
Filter system recycle-water rate is 83%, by chlorion and sulfate ion can efficiently separate, dish tubular type nanofiltration system
Concentrate sulfate ion content can be concentrated into 35000mg/L, and permeate chloride ion content is 18000mg/L.
The concentrate and permeate of nanofiltration system are respectively adopted the first and second counter-infiltration systems and carry out concentration again.Two
Set counter-infiltration system use 90bar hiigh pressure stage film posts, and diaphragm uses high to chlorion and sulfate ion rejection anti-
Permeate diaphragm.First counter-infiltration system recycle-water rate is 65.5%, sulfate ion content 102301.8mg/L after concentration, second
Counter-infiltration system recycle-water rate is 64.5%, chloride ion content 50908mg/L after concentration.The transmission hydroful of two sets of counter-infiltration systems
Sufficient reuse requirement, recycling.
After the chilled crystallization kettle 28 of concentrate and 1# centrifugal dehydrators 29 processing of first counter-infiltration system, acquisition purity >=
98% sal glauberi (saltcake), denitration liquid return to nanofiltration system water inlet end, reprocessed.Second counter-infiltration system it is dense
Contracting liquid obtains the sodium chloride crystal of purity >=94%, steam condensate (SC) after crystallizing evaporator 30 and 2# centrifugal dehydrators 31 are handled
Collect reuse.
Embodiment 3
Certain desulfurization wastewater project, handle water 15t/h, influent quality：pH：7.42, total dissolved solid (TDS)：
30000mg/L, Cl-：7860mg/L, SO4 2-：7530mg/L, Mg2+：800mg/L, Ca2+：1800mg/L, HCO3 -：10.9mg/L,
COD (COD)：450mg/L.
Processing requirement：Water outlet reaches circulating cooling water of power plant standard：pH:6-9, total dissolved solid (TDS)≤1000mg/
L, Cl-：≤ 250mg/L, SO4 2-：≤ 250mg/L, total hardness is (with CaCO3Meter)≤450mg/L, COD (COD)≤
50mg/L, effluent reuse divide salt, and waste water realizes zero discharge treatment.
From technique：
Softening pretreatment → ultrafiltration → Na-ion exchanger → nanofiltration divides salt → counter-infiltration → freezing and crystallizing and evaporative crystallization.
After the adjusted pond preliminary sedimentation processing of desulfurization wastewater, into 1# reactive tanks 1, adding mass concentration in 1# reactive tanks 1 is
40% sodium hydroxide solution 0.11t/h, make its pH value in 10-11, by the stirring of 1# agitators 2 make sodium hydroxide solution with it is de-
The abundant haptoreaction of sulphur waste water, hydraulic detention time 20 minutes, subsequently into 2# reactive tanks 3, continue to add matter in 2# reactive tanks 3
The sodium hydroxide solution that concentration is 40% is measured, control ph is 11 or so, while it is molten to add the sodium carbonate that mass concentration is 30%
Liquid 0.26t/h, stirred by 2# agitators 4, control hydraulic detention time 20 minutes, make medicament and the abundant haptoreaction of waste water,
And it is set to enter the concentration water tank 5 of ultrafiltration system with coagulation state.
Ultrafiltration system is designed as cross-flow filtration, and ultrafiltration intake pump 6 supplies water to hyperfiltration membrane assembly 7, by taking for milipore filter retention
Concentrate with a large amount of sediments returns to concentration water tank 5 and further circulation concentration is mixed with water, and the concentration sludge concentration of water tank 5 reaches
During to 3-4%, sludge condensation liquid is discharged to sludge concentration tank 11,11 hydraulic detention time of sludge concentration tank 12 hours, high power is dense
The sludge condensation liquid of contracting carries out press dewatering, caused mud cake is about with plate and frame filter press 12 from concentration trench bottom discharge to it
0.26t/h, sludge content is not less than 60%, pressure a small amount of in a small amount of supernatant and plate and frame filter press 12 in sludge concentration tank 11
Water is squeezed, then returns to 1# reactive tanks 1 and further handles.
The permeate hardness of ultrafiltration system is less than 100mg/L, and turbidity enters intermediate water tank 8 less than 1NTU, to intermediate water tank 8
The technical-grade hydrochloric acid that mass concentration is 30-37% is added, it is 7 or so to control its pH, is then entered by Na-ion exchanger intake pump 9
Enter Na-ion exchanger 10, further remove hardness, Na-ion exchanger 10, which goes out the water hardness, can be down to below 3mg/L.
Through except the water pre-processed firmly is through the entrance 1# of nanofiltration 1# intake pumps 13 accurate filters 14,1# accurate filters 14 filter
Precision is 10 μm, after removing impurity small in water removal, then after 1# high-pressure pumps 15 and 1# booster pumps 16 boost, into NF membrane group
Part 17, nanofiltration membrane component 17 select normal pressure level 75bar film posts, and diaphragm uses the extraordinary NF membrane dedicated for solventing-out.Receive
Filter system recycle-water rate is 78.5%, by chlorion and sulfate ion can efficiently separate, dish tubular type nanofiltration system
System concentrate sulfate ion content can be concentrated into 35000mg/L, and permeate chloride ion content is 10000mg/L.
The concentrate and permeate of nanofiltration system are respectively adopted the first and second counter-infiltration systems and carry out concentration again.Two
Set counter-infiltration system use 90bar hiigh pressure stage film posts, and diaphragm uses high to chlorion and sulfate ion rejection anti-
Permeate diaphragm.First counter-infiltration system recycle-water rate is 65.5%, sulfate ion content 101516.7mg/L after concentration, second
Counter-infiltration system recycle-water rate is 80%, chloride ion content 50100mg/L after concentration.The permeate of two sets of counter-infiltration systems meets
Reuse requirement, recycling.
After the chilled crystallization kettle 28 of concentrate and 1# centrifugal dehydrators 29 processing of first counter-infiltration system, acquisition purity >=
98.5% sal glauberi (saltcake), denitration liquid return to nanofiltration system water inlet end, reprocessed.Second counter-infiltration system
Concentrate obtains the sodium chloride crystal of purity >=94.8% after crystallizing evaporator 30 and 2# centrifugal dehydrators 31 are handled, and steam is cold
Condensed water collection reuse.
It is described above, only specific embodiment of the present utility model, but the scope of protection of the utility model is not limited to
In this, any one skilled in the art can readily occur in change in the technical scope that the utility model discloses
Or replace, it should all cover within the scope of protection of the utility model.Therefore, the scope of protection of the utility model should be with the power
The protection domain that profit requires is defined.
Claims (10)
- A kind of 1. device of desulfurization wastewater sub-prime crystallization treatment, it is characterised in that includingSoften pretreatment system,Ultra-filtration and separation system,Sludge treating system,Sodium ion melded system,Nanofiltration divides salt system,Counter-infiltration systemAnd crystal system,Desulfurization wastewater regulating reservoir is unidirectionally connected with the softening pretreatment system,The softening pretreatment system is unidirectionally connected with the ultra-filtration and separation systemThe ultra-filtration and separation system is unidirectionally connected with the sodium ion melded system, at the ultra-filtration and separation system and the sludge Reason system unidirectionally connects,The sludge treating system is unidirectionally connected with desulfurization wastewater regulating reservoir,The sodium ion melded system is unidirectionally connected with the nanofiltration point salt system,The nanofiltration point salt system is unidirectionally connected with the counter-infiltration system,The counter-infiltration system is unidirectionally connected with the crystal system.
- 2. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 1, it is characterised in that the softening pretreatment System includes the first reactive tank and the second reactive tank unidirectionally connected successively, desulfurization wastewater regulating reservoir and the first reactive tank list To connection, second reactive tank is unidirectionally connected with the ultra-filtration and separation system.
- 3. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 1, it is characterised in that the ultra-filtration and separation system System includes concentrating water tank, ultrafiltration intake pump, hyperfiltration membrane assembly and intermediate water tank, the softening pretreatment system and the condensed water Packing list is unidirectionally connected to connection, the concentration water tank with the ultrafiltration intake pump, the ultrafiltration intake pump and the intermediate water tank Unidirectional connection, the intermediate water tank and the condensed water packing list are to being connected, the intermediate water tank and the sodium ion melded system Unidirectional connection.
- 4. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 1, it is characterised in that the Treatment of Sludge system System includes sludge concentration tank and filter press, and the ultra-filtration and separation system is unidirectionally connected with the sludge concentration tank, and the sludge is dense Contracting groove is unidirectionally connected with the filter press, and the filter press is unidirectionally connected with the sofening treatment system.
- 5. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 1, it is characterised in that the sodium ion softening System includes the intake pump and Na-ion exchanger being sequentially connected, and the ultra-filtration and separation system is unidirectionally connected with the intake pump, The Na-ion exchanger is unidirectionally connected with the nanofiltration point salt system.
- 6. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 1, it is characterised in that the nanofiltration divides salt system Unite as dish tubular type nanofiltration point salt system, intake pump that the dish tubular type nanofiltration point salt system includes being sequentially connected, accurate filter, High-pressure plunger pump, booster pump and dish tubular nanofiltration membrane component, the sodium ion melded system are unidirectionally connected with the intake pump, institute Dish tubular nanofiltration membrane component is stated unidirectionally to be connected with the counter-infiltration system.
- 7. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 1, it is characterised in that the counter-infiltration system Including the first counter-infiltration system and the second counter-infiltration system, first counter-infiltration system and second counter-infiltration system are two Individual identical and mutually independent disc tube reverse osmosis (dt-ro) system, the nanofiltration divide salt system respectively with the disc tube reverse osmosis (dt-ro) system Unidirectional connection.
- 8. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 7, it is characterised in that the dish tubular type reverse osmosis Permeable system includes intake pump, accurate filter, high-pressure plunger pump, booster pump and the disc tube reverse osmosis (dt-ro) membrane module being sequentially connected, The nanofiltration point salt system is unidirectionally connected with the intake pump, and the disc tube reverse osmosis (dt-ro) membrane module and the crystal system are unidirectional Connection.
- 9. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 7, it is characterised in that the crystal system bag Include separate freezing and crystallizing system and evaporation and crystallization system, first counter-infiltration system and the freezing and crystallizing system list To connection, second counter-infiltration system is unidirectionally connected with the evaporation and crystallization system.
- 10. the device of desulfurization wastewater sub-prime crystallization treatment according to claim 9, it is characterised in that the freezing and crystallizing System includes the freezing and crystallizing kettle and centrifugal dehydrator being sequentially connected, and the evaporation and crystallization system includes the evaporation knot being sequentially connected Brilliant device and centrifugal dehydrator, first counter-infiltration system are unidirectionally connected with the freezing and crystallizing kettle, the second counter-infiltration system System is unidirectionally connected with the crystallizing evaporator.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110028187A (en) * | 2019-04-19 | 2019-07-19 | 四川思达能环保科技有限公司 | A kind of high-salt wastewater treatment process containing heavy metal |
| CN110877946A (en) * | 2019-12-24 | 2020-03-13 | 北京天地人环保科技有限公司 | Coking wastewater treatment method and system |
| CN111847742A (en) * | 2019-04-24 | 2020-10-30 | 中国石油化工股份有限公司 | Industrial wastewater treatment system and application thereof |
| CN111892215A (en) * | 2019-05-06 | 2020-11-06 | 中国石油化工股份有限公司 | Method for treating catalytic cracking flue gas desulfurization wastewater |
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2017
- 2017-05-09 CN CN201720510730.5U patent/CN206858347U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110028187A (en) * | 2019-04-19 | 2019-07-19 | 四川思达能环保科技有限公司 | A kind of high-salt wastewater treatment process containing heavy metal |
| CN111847742A (en) * | 2019-04-24 | 2020-10-30 | 中国石油化工股份有限公司 | Industrial wastewater treatment system and application thereof |
| CN111892215A (en) * | 2019-05-06 | 2020-11-06 | 中国石油化工股份有限公司 | Method for treating catalytic cracking flue gas desulfurization wastewater |
| CN110877946A (en) * | 2019-12-24 | 2020-03-13 | 北京天地人环保科技有限公司 | Coking wastewater treatment method and system |
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