CN108726770A - A kind of advanced treatment and reclamation method of flue gas desulfurization liquid - Google Patents
A kind of advanced treatment and reclamation method of flue gas desulfurization liquid Download PDFInfo
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- CN108726770A CN108726770A CN201710270162.0A CN201710270162A CN108726770A CN 108726770 A CN108726770 A CN 108726770A CN 201710270162 A CN201710270162 A CN 201710270162A CN 108726770 A CN108726770 A CN 108726770A
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- flue gas
- gas desulfurization
- water
- desulfurization liquid
- membrane distillation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- 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
- C02F1/048—Purification of waste water by 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
Abstract
The present invention relates to a kind of advanced treatment and reclamation methods of flue gas desulfurization liquid.This method is using efficiently except the advanced treatment and reclamation for realizing flue gas desulfurization liquid as hard as filter+membrane distillation+evaporative crystallization technique.The advanced treatment and reclamation of flue gas desulfurization liquid can be achieved in the present invention, on the basis of hardness in effectively removing doctor solution and suspended matter, realizes the recycling of water resource in flue gas desulfurization liquid, solves the problems, such as that flue gas desulfurization liquid processing is difficult in petroleum chemical enterprise.It is treated by the present method after formed system production water can direct reuse in recirculated water, realize the advanced treatment and reclamation of flue gas desulfurization liquid.
Description
Technical field
The present invention relates to field of industrial waste water treatment, specifically a kind of advanced treatment and reclamation method of flue gas desulfurization liquid.
Espespecially using efficiently except the advanced treatment and reclamation as hard as filter+membrane distillation+evaporative crystallization technique processing petroleum chemical enterprise flue gas desulfurization liquid
Method.
Background technology
As modern society continues to increase the consumption of fossil fuel, SOx and the atmosphere pollutions such as NOx and dust are also therewith
A large amount of to generate, these substances, which are largely discharged into air, will cause serious atmosphere pollution.SO2, NOx and particulate matter be emitted on China
There are stringent limitation, petro chemical industry pollutant emission standard (GB31571-2015) to require SO2Less than 100mg/m3, NOXIt is low
In 150mg/m3, particulate matter is less than 20mg/m3.It is taken off currently, the catalytic cracking unit of nearly all petroleum chemical enterprise all establishes flue gas
Sulphur system.
The EDV wet scrubbing technologies of the widely used Belco companies exploitation of Domestic Petrochemical Enterprises, the method is in effectively removing flue gas
In oxysulfide while the dust in flue gas can be eluted, but generate a large amount of doctor solution therewith.The processing of doctor solution
It is costly, in certain Large Scale Petrochemical Enterprises, usually it will be used as general wastewater treatment after doctor solution and other waste water mix and converts,
Though temporarily solving environmental issue, the problem of reusing sewage enterprise quality of reused water salt content gradually increases is easily led to, it is difficult to
Realize the salt balance of enterprise.Some enterprises are also individually handled doctor solution, such as using sodalime double alkali method, cycle sodium alkali technology
Take in alkali back and forth, but cost and long-term operation constrain the popularization and application of such technology.With petro chemical industry pollutant
The implementation of discharge standard (GB31571-2015), especially certain areas have stringent limitation, Beijing to the discharge of brine waste
It is required that soluble solids content is less than 1600mg/L, therefore the high concentration saliferous that EDV wet scrubbing technologies generate in efflux wastewater
There is emission treatment in doctor solution, it has also become technology uses a problem of unit.
It is effective method using the mating evaporation technique of dual-membrane process, patent 201510275955.2 uses nanofiltration
Desulfurization wastewater is handled with reverse osmosis embrane method group technology, then ion exchange, freezing and crystallizing and evaporation technology is used to realize salt
The separation and recovery of class, but that there are operating pressures is high, softening dosage is big, high energy consumption and system complex equipment are various for the technique
The problem of.Patent 201610038282.3 discloses a kind of power plant desulfurization wastewater processing system, nanofiltration, reverse osmosis and electric drive film
Combination, rear plus evaporative crystallization realize the processing of desulfurization wastewater, but there are processing units more, the problem of flow complexity.Patent
201010232059.5 handle sodium alkali flue gas desulfurization liquid using bipolar membrane electrodialysis method, realize the zero-emission of doctor solution, but should
System has that investment is high, energy consumption is big.
Invention content
In view of the deficiencies in the prior art, the purpose of the present invention is to provide a kind of advanced treatings of flue gas desulfurization liquid
Reuse method realizes the recycling of water resource in doctor solution on the basis of flue gas desulfurization liquid is effectively treated, and solves flue gas desulfurization liquid
In processing procedure the problem of suspension content height, high energy consumption, the final advanced treatment and reclamation for realizing flue gas desulfurization liquid.Through we
After method processing the fresh water that is formed can direct reuse in circulating cooling make-up water, realize the treatment for reuse of flue gas desulfurization liquid, while through we
The high-purity sulfuric acid sodium salt obtained after method processing, also can be used as utilization of the recycling of renewable resources.
To achieve the above objectives, the technical solution adopted by the present invention is that：
A kind of advanced treatment and reclamation method of flue gas desulfurization liquid, includes the following steps：
Step 1, flue gas desulfurization liquid, which enters, efficiently removes hard filter element, is added and removes hard medicament, reaction after a certain period of time, carries out
Membrane filtration is formed efficiently except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
Step 2, it efficiently forms membrane distillation production water except being concentrated as hard as filtering out water and enter membrane distillation unit and membrane distillation is dense
Water；
Step 3, membrane distillation concentrated water enters evaporative crystallization unit and is evaporated crystallization treatment, obtains salt crystalloid and evaporation is tied
Crystalline substance production water.
Based on the above technical solution, the membrane distillation production water and evaporative crystallization production water mixing are back to recirculated water benefit
Water.
Based on the above technical solution, the main water quality characteristic of the flue gas desulfurization liquid is：Total dissolved solid
55000~75000mg/L, 1000~2000mg/L of suspended matter, oil content 0~1mg/L, Cl-100~150mg/L, SO4 2-
35000~45000mg/L, Mg2+50~500mg/L, Ca2+100~1000mg/L, molten 2~6mg/L of silicon, total alkalinity 100~
1000mg/L。
Based on the above technical solution, the 1200 μ S/ of conductivity < of the membrane distillation production water and evaporative crystallization production water
Cm, COD < 60mg/L, Cl-< 200mg/L, total oil < 0.5mg/L, meet circulating cooling make-up water reuse standard.
Based on the above technical solution, the hard medicament that removes efficiently removed described in step 1 in hard filter element is hydrogen-oxygen
It is sodium hydroxide to change sodium and sodium carbonate, dosages distribution：Sodium carbonate is 9~13:1, the medicament reaction time is 15~30min, except hard
It is polytetrafluoroethylene (PTFE) that pH, which is controlled and efficiently removed the membrane material of hard filter element 10.8~11.5, and membrane aperture is 0.15~0.25 μm.
Based on the above technical solution, described in step 1 efficiently remove hard filter element filter pressure be 0.08~
0.15MPa, membrane flux are 200~400L/m2·h。
Based on the above technical solution, membrane distillation unit described in step 2 uses hollow fiber film assembly, membrane distillation
Form uses inner pressed vacuum membrane distillation, i.e. feeding liquid to enter in the fenestra of membrane distillation unit, the membrane module shell of membrane distillation unit
Journey vacuumizes.
Based on the above technical solution, the membrane material of membrane distillation unit described in step 2 is Kynoar, poly- four
Vinyl fluoride or polypropylene.
Based on the above technical solution, the waste heat such as waste heat of plant work may be used in membrane distillation unit described in step 2
For low-temperature heat source.
Based on the above technical solution, the service condition of membrane distillation unit described in step 2 is：Inlet flow-patterm be 7~
8, inflow temperature be 60~75 DEG C, feeding liquid side crossflow velocity be 0.6~1.2m/s, per-meate side vacuum degree be -0.075~-
0.085MPa；With this condition, the membrane flux of membrane distillation unit is 5~10L/m2The TDS controls of h, membrane distillation concentrated water exist
200000mg/L。
Based on the above technical solution, evaporative crystallization unit described in step 3 uses existing commercially available crystallizing evaporator,
Heat source is heated using exhaust steam or electrical heating.
The essential distinction of the present invention and the prior art is：For the technological deficiency of the prior art, the present invention is using high
Effect is except as hard as filter+membrane distillation+evaporative crystallization technique processing flue gas desulfurization liquid.By using the technology, it is useless to be effectively utilized low temperature
Heat realizes the advanced treatment and reclamation of flue gas desulfurization liquid.Compared to the prior art, technical equipment operation and maintenance of the present invention
Easy, strong environmental adaptability, achievable skid processing, Technical Economy are good.
Advantageous effect：
1, the present invention is using hard filtration treatment flue gas desulfurization liquid is efficiently removed, efficiently except as hard as filter and efficient sedimentation tank, precision
Filtering technique is compared, and technical equipment of the present invention is simple, high degree of automation, strong environmental adaptability, floor space are few,
And organic film anti-pollution ability is strong, flux is big；
2, the present invention handles flue gas desulfurization liquid using film distillation technology, takes full advantage of factory's low-temperature waste heat, and using steaming
It sends out crystallization technique and handles membrane distillation concentrated water, take full advantage of the waste heat of membrane distillation concentrated water, reduce operating cost；
3, method using the present invention carries out the advanced treatment and reclamation of flue gas desulfurization liquid, solves petroleum chemical enterprise's flue gas desulfurization
The difficult problem of liquid processing, while realizing water resource reuse.
Description of the drawings
The present invention has following attached drawing：
The process flow chart of Fig. 1 present invention.
Specific implementation mode
Below in conjunction with attached drawing, invention is further described in detail.
As shown in Figure 1, the advanced treatment and reclamation method of flue gas desulfurization liquid of the present invention, using " efficiently except as hard as filter+
Membrane distillation+evaporative crystallization " technology path, includes the following steps：
Step 1, flue gas desulfurization liquid, which enters, efficiently removes hard filter element, is added and removes hard medicament, reaction after a certain period of time, carries out
Membrane filtration is formed efficiently except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
Step 2, it efficiently forms membrane distillation production water except being concentrated as hard as filtering out water and enter membrane distillation unit and membrane distillation is dense
Water；
Step 3, membrane distillation concentrated water enters evaporative crystallization unit and is evaporated crystallization treatment, obtains salt crystalloid and evaporation is tied
Crystalline substance production water.
Based on the above technical solution, the membrane distillation production water and evaporative crystallization production water mixing are back to recirculated water benefit
Water.
Based on the above technical solution, the main water quality characteristic of the flue gas desulfurization liquid is：Total dissolved solid
55000~75000mg/L, 1000~2000mg/L of suspended matter, oil content 0~1mg/L, Cl-100~150mg/L, SO4 2-
35000~45000mg/L, Mg2+50~500mg/L, Ca2+100~1000mg/L, molten 2~6mg/L of silicon, total alkalinity 100~
1000mg/L。
Based on the above technical solution, the 1200 μ S/ of conductivity < of the membrane distillation production water and evaporative crystallization production water
Cm, COD < 60mg/L, Cl-< 200mg/L, total oil < 0.5mg/L, meet circulating cooling make-up water reuse standard.
Based on the above technical solution, the hard medicament that removes efficiently removed described in step 1 in hard filter element is hydrogen-oxygen
It is sodium hydroxide to change sodium and sodium carbonate, dosages distribution：Sodium carbonate is 9~13:1, the medicament reaction time is 15~30min, except hard
It is polytetrafluoroethylene (PTFE) that pH, which is controlled and efficiently removed the membrane material of hard filter element 10.8~11.5, and membrane aperture is 0.15~0.25 μm.
Based on the above technical solution, described in step 1 efficiently remove hard filter element filter pressure be 0.08~
0.15MPa, membrane flux are 200~400L/m2·h。
Based on the above technical solution, membrane distillation unit described in step 2 uses hollow fiber film assembly, membrane distillation
Form uses inner pressed vacuum membrane distillation, i.e. feeding liquid to enter in the fenestra of membrane distillation unit, the membrane module shell of membrane distillation unit
Journey vacuumizes.
Based on the above technical solution, the membrane material of membrane distillation unit described in step 2 is Kynoar, poly- four
Vinyl fluoride or polypropylene.
Based on the above technical solution, the waste heat such as waste heat of plant work may be used in membrane distillation unit described in step 2
For low-temperature heat source.
Based on the above technical solution, the service condition of membrane distillation unit described in step 2 is：Inlet flow-patterm be 7~
8, inflow temperature be 60~75 DEG C, feeding liquid side crossflow velocity be 0.6~1.2m/s, per-meate side vacuum degree be -0.075~-
0.085MPa；With this condition, the membrane flux of membrane distillation unit is 5~10L/m2The TDS controls of h, membrane distillation concentrated water exist
200000mg/L, membrane distillation production water are back to circulating cooling make-up water.
Based on the above technical solution, evaporative crystallization unit described in step 3 uses existing commercially available crystallizing evaporator,
Heat source is heated using exhaust steam or electrical heating.
Embodiment 1
The main water quality characteristic of flue gas desulfurization liquid is：Total dissolved solid 55000mg/L, suspended matter 1000mg/L, Cl-
100mg/L, SO4 2-35000mg/L, Mg2+50mg/L, Ca2+100mg/L, molten silicon 2mg/L, total alkalinity 100mg/L.
Processing step is as follows：
Step 1, flue gas desulfurization liquid, which enters, efficiently removes hard filter element, is added and removes hard medicament sodium hydroxide and sodium carbonate, medicine
Agent proportioning is sodium hydroxide：Sodium carbonate is 9:1, except hard pH controls are 10.8,15min is reacted, carries out membrane filtration later, formed high
Effect is except as hard as filtering out water；The filter pressure for efficiently removing hard filter element is 0.08MPa, and membrane material is polytetrafluoroethylene (PTFE), membrane aperture
0.15μm；Outward transport processing is concentrated after filter residue class is cured；
With this condition, the membrane flux for efficiently removing hard filter element is 400L/m2·h；Efficiently except small as hard as water SS is filtered out
In 0.5mg/L, goes out the water hardness and be less than 80mg/L；
Step 2, it efficiently forms membrane distillation production water except being concentrated as hard as filtering out water and enter membrane distillation unit and membrane distillation is dense
Water；The membrane material of membrane distillation unit is polytetrafluoroethylene (PTFE), and service condition is inlet flow-patterm 7, and inflow temperature is 60 DEG C, feeding liquid side
Crossflow velocity is 1.2m/s, and per-meate side vacuum degree is -0.085MPa；
With this condition, the membrane flux of membrane distillation unit is 5L/m2H or so, membrane distillation concentrated water are controlled in TDS
200000mg/L, membrane distillation produce water conductivity < 1200 μ S/cm, Cl-< 200mg/L, total oil < 0.5mg/L, meet recirculated water
Moisturizing reuse standard；
Step 3, membrane distillation concentrated water enters evaporative crystallization unit and is evaporated crystallization treatment, obtains salt crystalloid and evaporation is tied
Crystalline substance production water；Evaporative crystallization production water also meets circulating cooling make-up water standard.
Embodiment 2
The main water quality characteristic of flue gas desulfurization liquid is：Total dissolved solid 65000mg/L, suspended matter 1500mg/L, oil contain
Measure 0.5mg/L, Cl-120mg/L, SO4 2-40000mg/L, Mg2+200mg/L, Ca2+500mg/L, molten silicon 4mg/L, total alkalinity
500mg/L。
Processing step is as follows：
Step 1, flue gas desulfurization liquid, which enters, efficiently removes hard filter element, is added and removes hard medicament sodium hydroxide and sodium carbonate, medicine
Agent proportioning is sodium hydroxide：Sodium carbonate is 11:1, except hard pH controls are 11.2,20min is reacted, carries out membrane filtration later, is formed
Efficiently except as hard as filtering out water；The filter pressure for efficiently removing hard filter element is 0.12MPa, and membrane material is polytetrafluoroethylene (PTFE), fenestra
0.2 μm of diameter；Outward transport processing is concentrated after filter residue class is cured；
With this condition, the membrane flux for efficiently removing hard filter element is 300L/m2·h；Efficiently except small as hard as water SS is filtered out
In 0.5mg/L, goes out the water hardness and be less than 80mg/L；
Step 2, it efficiently forms membrane distillation production water except continuing to concentrate as hard as filtering out water and enter membrane distillation unit and membrane distillation is dense
Water；The membrane material of membrane distillation unit is polypropylene, and service condition is inlet flow-patterm 7.5, and inflow temperature is 70 DEG C, feeding liquid side form
Surface current speed is 0.6m/s, and per-meate side vacuum degree is -0.08MPa；
With this condition, the membrane flux of membrane distillation unit is 8L/m2H, the TDS controls of membrane distillation concentrated water are in 200000mg/
L, membrane distillation produce water conductivity < 1200 μ S/cm, Cl-< 200mg/L, total oil < 0.5mg/L, meet circulating cooling make-up water reuse mark
It is accurate；
Step 3, membrane distillation concentrated water enters evaporative crystallization unit and is evaporated crystallization treatment, obtains salt crystalloid and evaporation is tied
Crystalline substance production water；Evaporative crystallization production water also meets circulating cooling make-up water standard.
Embodiment 3
The main water quality characteristic of flue gas desulfurization liquid is：Total dissolved solid 75000mg/L, suspended matter 2000mg/L, oil contain
Measure 1mg/L, Cl-150mg/L, SO4 2-45000mg/L, Mg2+500mg/L, Ca2+1000mg/L, molten silicon 6mg/L, total alkalinity
1000mg/L。
Processing step is as follows：
Step 1, flue gas desulfurization liquid, which enters, efficiently removes hard filter element, is added and removes hard medicament sodium hydroxide and sodium carbonate, medicine
Agent proportioning is sodium hydroxide：Sodium carbonate is 13:1, except hard pH controls are 11.5,30min is reacted, carries out membrane filtration later, is formed
Efficiently except as hard as filtering out water；The filter pressure for efficiently removing hard filter element is 0.15MPa, and membrane material is polytetrafluoroethylene (PTFE), fenestra
0.25 μm of diameter；Outward transport processing is concentrated after filter residue class is cured；
With this condition, the membrane flux for efficiently removing hard filter element is 200L/m2·h；Efficiently except small as hard as water SS is filtered out
In 0.5mg/L, goes out the water hardness and be less than 80mg/L；
Step 2, it efficiently forms membrane distillation production water except continuing to concentrate as hard as filtering out water and enter membrane distillation unit and membrane distillation is dense
Water；The membrane material of membrane distillation unit is Kynoar, and service condition is inlet flow-patterm 8, and inflow temperature is 75 DEG C, feeding liquid side
Crossflow velocity is 0.8m/s, and per-meate side vacuum degree is -0.075MPa；
With this condition, the membrane flux of membrane distillation unit is 10L/m2H, the TDS controls of membrane distillation concentrated water are in 200000mg/
L, membrane distillation produce water conductivity < 1200 μ S/cm, Cl-< 200mg/L, total oil < 0.5mg/L, meet circulating cooling make-up water reuse mark
It is accurate；
Step 3, membrane distillation concentrated water enters evaporative crystallization unit and is evaporated crystallization treatment, obtains salt crystalloid and evaporation is tied
Crystalline substance production water；Evaporative crystallization production water also meets circulating cooling make-up water standard.
The foregoing is merely the preferable possible embodiments of the present invention, not thereby limit to the scope of the claims of the present invention, therefore all
It is to be both contained in protection scope of the present invention with equivalence changes made by description of the invention and accompanying drawing content.
The content not being described in detail in this specification belongs to the prior art well known to professional and technical personnel in the field.
Claims (10)
1. a kind of advanced treatment and reclamation method of flue gas desulfurization liquid, it is characterised in that：Include the following steps：
Step 1, flue gas desulfurization liquid, which enters, efficiently removes hard filter element, is added and removes hard medicament, reaction after a certain period of time, carries out film mistake
Filter is formed efficiently except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
Step 2, membrane distillation production water and membrane distillation concentrated water efficiently are formed except being concentrated as hard as filtering out water and enter membrane distillation unit；
Step 3, membrane distillation concentrated water enters evaporative crystallization unit and is evaporated crystallization treatment, obtains salt crystalloid and evaporative crystallization production
Water.
2. the advanced treatment and reclamation method of flue gas desulfurization liquid as described in claim 1, it is characterised in that：The flue gas desulfurization liquid
Main water quality characteristic be：55000~75000mg/L of total dissolved solid, 1000~2000mg/L of suspended matter, oil content 0~
1mg/L, Cl-100~150mg/L, SO4 2-35000~45000mg/L, Mg2+50~500mg/L, Ca2+100~1000mg/L, it is molten
2~6mg/L of silicon, 100~1000mg/L of total alkalinity.
3. the advanced treatment and reclamation method of flue gas desulfurization liquid as described in claim 1, it is characterised in that：It is high described in step 1
Effect is except, except hard medicament is sodium hydroxide and sodium carbonate, dosages distribution is sodium hydroxide in hard filter element：Sodium carbonate be 9~
13:1, the medicament reaction time is 15~30min, except hard pH is controlled 10.8~11.5, efficiently removes the membrane material of hard filter element
For polytetrafluoroethylene (PTFE), membrane aperture is 0.15~0.25 μm.
4. the advanced treatment and reclamation method of flue gas desulfurization liquid as described in claim 1, it is characterised in that：It is high described in step 1
Effect is 0.08~0.15MPa except the filter pressure of hard filter element, and membrane flux is 200~400L/m2·h。
5. the advanced treatment and reclamation method of flue gas desulfurization liquid as described in claim 1, it is characterised in that：Film described in step 2
Distillation unit uses hollow fiber film assembly, membrane distillation form that inner pressed vacuum membrane distillation, feeding liquid is used to enter membrane distillation list
In the fenestra of member, the membrane module shell side of membrane distillation unit vacuumizes；The membrane material of the membrane distillation unit is Kynoar, gathers
Tetrafluoroethene or polypropylene.
6. the advanced treatment and reclamation method of flue gas desulfurization liquid as claimed in claim 5, it is characterised in that：Film described in step 2
The service condition of distillation unit is：Inlet flow-patterm be 7~8, inflow temperature be 60~75 DEG C, feeding liquid side crossflow velocity be 0.6~
1.2m/s, per-meate side vacuum degree are -0.075~-0.085MPa；With this condition, the membrane flux of membrane distillation unit is 5~10L/
m2The TDS of h, membrane distillation concentrated water are controlled in 200000mg/L.
7. the advanced treatment and reclamation method of flue gas desulfurization liquid as claimed in claim 6, it is characterised in that：Film described in step 2
Distillation unit is using waste heat of plant as low-temperature heat source.
8. the advanced treatment and reclamation method of flue gas desulfurization liquid as described in claim 1, it is characterised in that：It is steamed described in step 3
It sends out crystalline element and uses existing commercially available crystallizing evaporator, heat source is heated using exhaust steam or electrical heating.
9. the advanced treatment and reclamation method of flue gas desulfurization liquid as described in claim 1, it is characterised in that：The membrane distillation produces water
Conductivity < 1200 μ S/cm, COD the < 60mg/L, Cl of water are produced with evaporative crystallization-< 200mg/L, total oil < 0.5mg/L, meet
Circulating cooling make-up water reuse standard.
10. the advanced treatment and reclamation method of flue gas desulfurization liquid as claimed in claim 9, it is characterised in that：The membrane distillation production
Water and evaporative crystallization production water mixing are back to circulating cooling make-up water.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111167317A (en) * | 2020-01-15 | 2020-05-19 | 上海翊科精密挤出技术有限公司 | Preparation of high-hydrophobicity hollow fiber membrane and desulfurization wastewater treatment method thereof |
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