CN205974141U - Desulphurization waste water treatment system - Google Patents
Desulphurization waste water treatment system Download PDFInfo
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- CN205974141U CN205974141U CN201621018421.8U CN201621018421U CN205974141U CN 205974141 U CN205974141 U CN 205974141U CN 201621018421 U CN201621018421 U CN 201621018421U CN 205974141 U CN205974141 U CN 205974141U
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- evaporation
- subsystem
- water
- desulfurization wastewater
- upgrading unit
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- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 57
- 238000001704 evaporation Methods 0.000 claims abstract description 49
- 230000003009 desulfurizing Effects 0.000 claims abstract description 41
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 39
- 238000002425 crystallisation Methods 0.000 claims abstract description 34
- 230000005712 crystallization Effects 0.000 claims abstract description 34
- 239000012528 membrane Substances 0.000 claims abstract description 29
- 239000002351 wastewater Substances 0.000 claims abstract description 25
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 150000003839 salts Chemical class 0.000 claims abstract description 6
- 239000011780 sodium chloride Substances 0.000 claims abstract description 6
- 238000001728 nano-filtration Methods 0.000 claims description 29
- 238000001223 reverse osmosis Methods 0.000 claims description 20
- 238000001471 micro-filtration Methods 0.000 claims description 16
- 239000006200 vaporizer Substances 0.000 claims description 5
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium monoxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 15
- 239000000243 solution Substances 0.000 description 9
- 239000000463 material Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 235000002639 sodium chloride Nutrition 0.000 description 5
- 238000000926 separation method Methods 0.000 description 4
- 238000007906 compression Methods 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 230000003204 osmotic Effects 0.000 description 3
- 238000004094 preconcentration Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 210000004940 Nucleus Anatomy 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000010442 halite Substances 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000000967 suction filtration Methods 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
Abstract
The utility model discloses a desulphurization waste water treatment system relates to the water treatment field. The system includes pretreatment systems, membrane processing system and evaporation crystal system, pretreatment systems, membrane processing system and evaporation crystal system are arranged in proper order, pretreatment systems is used for carrying out the preliminary treatment to desulfurization waste water, membrane processing system is used for carrying out the advanced treatment to the desulfurization waste water after the preliminary treatment, the evaporation crystal system is used for evaporating the crystallization and obtaining salt crystal membrane processing system concentrate. The utility model discloses a zero release will have mode of processing effective combination now, realize that desulfurization waste water divides the matter retrieval and utilization, reduces the running cost.
Description
Technical field
This utility model is related to water treatment field, more particularly, to a kind of desulfurization wastewater treatment system.
Background technology
Existing method carries out producing a certain amount of desulfurization wastewater, desulfurization during desulfurization process to the flue gas that coal-burning utilities produce
Waste water huge to environmental hazard it is necessary to strictly be processed.And, with the continuous improvement of environmental requirement, advanced treating, reuse take off
Sulfur waste water, realizes a kind of trend that wastewater zero discharge is that desulfurization wastewater is processed.
Technique of zero discharge species is various, common are direct evaporation, flue gas evaporation, membrane separating method, electrodialysis, just oozes
Thoroughly, film combination, MVR etc., respectively have pluses and minuses.Such as evaporation technique is direct, effective, but consumption quantity of steam or power consumption are greatly, investment
High with operating cost；Flue evaporation technique, energy consumption is relatively low, but increases smoke moisture, affects dust pelletizing system, corrosion and scaling risk
Increase；Membrance separation, such as nanofiltration, reverse osmosiss, method is stably simple, but less efficient, operating pressure is high, be not fee from fouling membrane；
Electrodialytic technique investment is big, application fee is high；Just permeating and belonging to new technique, effect is fine, but complex process, technology maturity are relatively
Low and energy consumption is higher.MVR is the energy of the indirect steam of re-using vaporized device, thus reducing the one of the demand of the energy to external world
Item technology.Its work process is that the steam of low temperature position compresses through compressor, and temperature, pressure improve, and heat content increases, subsequently into changing
Hot device condensation, to make full use of the latent heat of steam.In addition to start up, without primary steam in whole evaporation process, but, MVR
High cost.
Utility model content
The purpose of this utility model is to provide a kind of desulfurization wastewater treatment system, thus solving present in prior art
Foregoing problems.
To achieve these goals, desulfurization wastewater treatment system described in the utility model, described system includes pretreatment system
System, film processing system and evaporation and crystallization system；Described pretreatment system, film processing system and evaporation and crystallization system are sequentially arranged；
Described pretreatment system is used for desulfurization wastewater is carried out pretreatment, and described film processing system is used for pretreated
Desulfurization wastewater carries out advanced treating, and described evaporation and crystallization system is used for film processing system concentrated solution being evaporated crystallizing and obtaining
Crystal salt；
Described film processing system includes microfiltration processing subsystem, nanofiltration processing subsystem and the reverse osmosiss subsystem being sequentially arranged
System；Described microfiltration processing subsystem is used for processing the waste water of preprocessed system institute pretreatment, described microfiltration processing subsystem
Produce water and enter nanofiltration processing subsystem；The product water of described nanofiltration processing subsystem enters reverse osmosiss subsystem；Described reverse osmosiss
The fresh water of system enters fresh-water tank, and the concentrated solution of described reverse osmosiss subsystem enters evaporation and crystallization system；
Reverse osmosis membrane upgrading unit that described reverse osmosiss subsystem includes being sequentially arranged, seawater reverse osmosis membrane upgrading unit and
DTRO upgrading unit；The product water of described nanofiltration processing subsystem enters reverse osmosis membrane upgrading unit, reverse osmosis membrane upgrading unit
Concentrated water enters seawater reverse osmosis membrane upgrading unit, and the concentrated water of described seawater reverse osmosis membrane upgrading unit enters described DTRO and concentrates list
Unit, the fresh water of described DTRO upgrading unit enters fresh-water tank, and the concentrated solution of described DTRO upgrading unit enters evaporation and crystallization system.
Preferably, the thickened sludge of described microfiltration processing subsystem is back to pretreatment system, nanofiltration processing subsystem
Concentrated solution is back to pretreatment system.
Preferably, described microfiltration processing subsystem adopts tube type filter membrance.
Preferably, described nanofiltration processing subsystem is one-level nanofiltration device or the combination of multistage nanofiltration device.
Preferably, described pretreatment system is Calx melded system.
Preferably, used in described evaporation and crystallization system, compressor is Roots Compressor.
Preferably, used in described evaporation and crystallization system, heater is shell-and-tube heat exchanger.
Preferably, described evaporation and crystallization system is also associated with outside steam engine, and the steam that steam engine produces enters described steaming
Send out in the vaporizer of crystal system.
The beneficial effects of the utility model are that this utility model achieves zero-emission, by existing processing mode efficient combination,
Realize desulfurization wastewater separate-recycling, reduce operating cost.
1st, desulfurization wastewater treatment system provided by the present invention has coupled materializing strategy and membrane technology, improves system
The stability run；
2nd, desulfurization wastewater treatment system provided by the present invention adopts nanofiltration processing system to the bivalence in desulfurization wastewater
Ion carries out separating, it is achieved thereby that the separate-recycling of desulfurization wastewater, improves the reclamation rate of water；
3rd, in desulfurization wastewater treatment system provided by the present invention the NF concentrated water reuse of nanofiltration processing system to desulphurization system
In desulfurizing tower, the recycling condensing water of evaporation and crystallization system, evaporation and crystallization system produce crystal salt can as Nacl, thus
Achieve the zero-emission effect of waste water, there is preferable social value and the value of environmental protection.
Brief description
Fig. 1 is the structural representation of described desulfurization wastewater treatment system.
Specific embodiment
In order that the purpose of this utility model, technical scheme and advantage become more apparent, below in conjunction with accompanying drawing, to this reality
It is further elaborated with new.It should be appreciated that specific embodiment described herein is only in order to explain this practicality
New, it is not used to limit this utility model.
Embodiment
With reference to Fig. 1, desulfurization wastewater treatment system described in the present embodiment, described system includes pretreatment system 1, film process system
System 2 and evaporation and crystallization system 3；Described pretreatment system 1, film processing system 2 and evaporation and crystallization system 3 are sequentially arranged；
Described pretreatment system 1 is used for desulfurization wastewater is carried out pretreatment, after described film processing system 2 is used for pretreatment
Desulfurization wastewater carry out advanced treating, described evaporation and crystallization system 3 is used for film processing system concentrated solution being evaporated with crystallization simultaneously
Obtain crystal salt；
Described film processing system 2 includes microfiltration processing subsystem 21, nanofiltration processing subsystem 22 and the reverse osmosis being sequentially arranged
Subsystem 23 thoroughly；Described microfiltration processing subsystem 21 is used for processing the waste water of preprocessed system institute pretreatment, at described microfiltration
The product water of reason subsystem 21 enters nanofiltration processing subsystem；The product water of described nanofiltration processing subsystem 22 enters reverse osmosiss subsystem
System；The product water of described reverse osmosiss subsystem 23 enters fresh-water tank 4, and the concentrated solution of described reverse osmosiss subsystem 22 enters evaporative crystallization
System 3；
Described reverse osmosiss subsystem 23 includes reverse osmosis membrane upgrading unit 231, the sea-water reverse osmose membrance concentration being sequentially arranged
Unit 232 and DTRO upgrading unit 233；The product water of described nanofiltration processing subsystem 22 enters reverse osmosis membrane upgrading unit 231, instead
The product water of permeable membrane upgrading unit 231 enters seawater reverse osmosis membrane upgrading unit 232, described seawater reverse osmosis membrane upgrading unit
232 product water enters described DTRO upgrading unit 233, and the product water of described DTRO upgrading unit 233 enters fresh-water tank 4, described
The concentrated solution of DTRO upgrading unit 233 enters evaporation and crystallization system 3.
Explanation is explained in more detail is：
(1) thickened sludge of described microfiltration processing subsystem 21 is back to pretreatment system, nanofiltration processing subsystem 22
Concentrated solution is back to pretreatment system 1.
Reverse osmosis membrane upgrading unit 231, seawater reverse osmosis membrane upgrading unit 232, DTRO upgrading unit 233 and evaporative crystallization
System 3 all can produce fresh water and concentrated water, and the fresh water of generation all enters in fresh-water tank, and the concentrated water producing in each unit or system
Next step can be directly entered process.
(2) described pretreatment system 1 is Calx melded system.
Described microfiltration processing subsystem adopts tube type filter membrance.Described nanofiltration processing subsystem is one-level nanofiltration device or many
Level nanofiltration device combination.The separating mechanism of described NF membrane is screening and dissolving is spread and deposited, and has electrical charge rejection effect simultaneously again
Should, can effectively remove bivalence and multivalent ion, remove all kinds of materials that molecular weight is more than 200, can partly remove unit price from
The son and molecular weight material less than 200；First the remaining calcium and magnesium in washing water is removed with nanofiltration, during the water of the dilute side of output enters
Between water tank, can enter in reverse osmosiss pre-concentration technique.
(3) in reverse osmosiss pre-concentration technique, with pressure differential as motive force, it is a kind of film isolating solvent from solution
Lock out operation, because it is in opposite direction with naturally osmotic, therefore claims reverse osmosiss.Different osmotic according to various materials so that it may
Using the reverse osmosis pressure more than osmotic pressure, i.e. hyperfiltration, to reach separation, the purpose of extraction, purification and concentration.Through removing
Remove the water of hardness, reverse osmosiss can be directly entered, by reverse osmosiss pre-concentration, washing water can be concentrated into 6% 8%.Output light
Water can enter water wash system water scouring water.
(4) with regard to evaporation and crystallization system
1. raw water concentrate after Halite water as stock solution through pressurization preheating enter crystallizing evaporator unit, material total amount by
The liquidometer of crystallizer controls, and using double flange differential pressure levelmeters, controls to adjust feedstock valve.
2. in crystallizer, temperature of charge and evaporating temperature are determined by the setting value of compressor, under the temperature conditionss setting
Evaporation.
3. material heated device heating, in liquid level surface evaporation, produces maximum degree of supersaturation, due to there being substantial amounts of crystalline substance simultaneously
Grain together circulates with liquid, with the presence of substantial amounts of crystal grain during liquid surface evaporation, makes degree of supersaturation consumption in grain growth, it is to avoid
Spontaneously form nucleus.
4. used in described evaporation and crystallization system, heater is shell-and-tube heat exchanger, single tube journey, and tube side medium is material, shell
Cheng Jiezhi is the indirect steam after compression.Shell-and-tube heat exchanger is material heater, is also the condenser of indirect steam simultaneously.Institute
Stating circulating pump used in evaporation and crystallization system is big flow, the mixed-flow pump of low lift.
5., after multiple circulating and evaporating, skimming, vapor-liquid separation, moisture is evaporated out.
6. the compressor of vapor compression system is Roots Compressor, and compressed media is the secondary steaming producing in vaporizer
Vapour, indirect steam enters the heater tube side of vaporizer after compression, and there undergoes phase transition, and is changed into vapour after release heat
Solidifying water.
7. condensed water enters into condensate water pot and collects, and is used for MVR internal system spraying cooling by a condensate pump part,
It is partly into condensation water recovery system.
8. described evaporation and crystallization system is also associated with outside steam engine, and the steam starting outside steam engine acquisition is directly entered
To vaporizer, after producing indirect steam, stop steam supply；
9. when using, all devices in evaporation and crystallization system and system interior conduit are set a low spot emission point, when being
When system exception or needs to carry out minimum point discharge, drain into the emission point specified.
The nearly saturation water yield is also less, so selecting forced circulation because dope has been concentrated into for system described in the utility model
Crystallizing evaporator, dope enters evaporating chamber, and heat exchanger is passed through live steam and dope is heated, the two of output in dope evaporation process
Section steam can enter Roots's vapor recompression machine and steam temperature rise is gone successively to heat exchanger to dope heating evaporation, need not persistently mend
Fill original vol saturated vapor, dope is evaporated reaching hypersaturated state precipitation crystal, then be discharged into suction filtration tank from evaporating chamber
Carry out solid-liquid separation, mother solution returns to evaporating chamber and continues evaporative crystallization.
By using technique scheme disclosed in this utility model, having obtained following beneficial effect：This utility model
Achieve zero-emission, existing processing mode efficient combination is realized desulfurization wastewater separate-recycling, reduced operating cost.
1st, desulfurization wastewater treatment system provided by the present invention has coupled materializing strategy and membrane technology, improves system
The stability run；
2nd, desulfurization wastewater treatment system provided by the present invention adopts nanofiltration processing system to the bivalence in desulfurization wastewater
Ion carries out separating, it is achieved thereby that the separate-recycling of desulfurization wastewater, improves the reclamation rate of water；
3rd, in desulfurization wastewater treatment system provided by the present invention the NF concentrated water reuse of nanofiltration processing system to desulphurization system
In desulfurizing tower, the recycling condensing water of evaporation and crystallization system, evaporation and crystallization system produce crystal salt can as Nacl, thus
Achieve the zero-emission effect of waste water, there is preferable social value and the value of environmental protection.
The above is only preferred implementation of the present utility model it is noted that common skill for the art
For art personnel, on the premise of without departing from this utility model principle, some improvements and modifications can also be made, these improve and
Retouching also should regard protection domain of the present utility model.
Claims (8)
1. a kind of desulfurization wastewater treatment system is it is characterised in that described system includes pretreatment system, film processing system and evaporation
Crystal system；Described pretreatment system, film processing system and evaporation and crystallization system are sequentially arranged；
Described pretreatment system is used for desulfurization wastewater is carried out pretreatment, and described film processing system is used for pretreated desulfurization
Waste water carries out advanced treating, and described evaporation and crystallization system is used for film processing system concentrated solution being evaporated crystallizing and being crystallized
Salt；
Described film processing system includes microfiltration processing subsystem, nanofiltration processing subsystem and the reverse osmosiss subsystem being sequentially arranged；
Described microfiltration processing subsystem is used for processing the waste water of preprocessed system institute pretreatment, the product water of described microfiltration processing subsystem
Enter nanofiltration processing subsystem；The product water of described nanofiltration processing subsystem enters reverse osmosiss subsystem；Described reverse osmosiss subsystem
Fresh water enter fresh-water tank, the concentrated solution of described reverse osmosiss subsystem enters evaporation and crystallization system；
Described reverse osmosiss subsystem includes reverse osmosis membrane upgrading unit, seawater reverse osmosis membrane upgrading unit and the DTRO being sequentially arranged
Upgrading unit；The product water of described nanofiltration processing subsystem enters reverse osmosis membrane upgrading unit, the concentrated water of reverse osmosis membrane upgrading unit
Enter seawater reverse osmosis membrane upgrading unit, the concentrated water of described seawater reverse osmosis membrane upgrading unit enters described DTRO upgrading unit,
The fresh water of described DTRO upgrading unit enters fresh-water tank, and the concentrated solution of described DTRO upgrading unit enters evaporation and crystallization system.
2. according to claim 1 desulfurization wastewater treatment system it is characterised in that the concentration of described microfiltration processing subsystem is dirty
Mud is back to pretreatment system, and the concentrated solution of nanofiltration processing subsystem is back to pretreatment system.
3. according to claim 1 desulfurization wastewater treatment system it is characterised in that described microfiltration processing subsystem adopts tubular type
Micro-filtration membrane.
4. according to claim 1 desulfurization wastewater treatment system it is characterised in that described nanofiltration processing subsystem is received for one-level
Filter device or the combination of multistage nanofiltration device.
5. according to claim 1 desulfurization wastewater treatment system it is characterised in that described pretreatment system be Calx softening system
System.
6. according to claim 1 desulfurization wastewater treatment system it is characterised in that used in described evaporation and crystallization system press
Contracting machine is Roots Compressor.
7. according to claim 1 desulfurization wastewater treatment system it is characterised in that used in described evaporation and crystallization system plus
Hot device is shell-and-tube heat exchanger.
8. according to claim 1 desulfurization wastewater treatment system it is characterised in that described evaporation and crystallization system be also associated with outer
Portion's steam engine, the steam that steam engine produces enters in the vaporizer of described evaporation and crystallization system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621018421.8U CN205974141U (en) | 2016-08-30 | 2016-08-30 | Desulphurization waste water treatment system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621018421.8U CN205974141U (en) | 2016-08-30 | 2016-08-30 | Desulphurization waste water treatment system |
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| CN205974141U true CN205974141U (en) | 2017-02-22 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107381922A (en) * | 2017-08-29 | 2017-11-24 | 大唐（北京）水务工程技术有限公司 | A kind of desulfurizing waste water processing device and smoke processing system |
-
2016
- 2016-08-30 CN CN201621018421.8U patent/CN205974141U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107381922A (en) * | 2017-08-29 | 2017-11-24 | 大唐（北京）水务工程技术有限公司 | A kind of desulfurizing waste water processing device and smoke processing system |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |