CN105254096A - Preprocessing method and device for gasification ammonia-cyanide-phenol-contained circulating water - Google Patents
Preprocessing method and device for gasification ammonia-cyanide-phenol-contained circulating water Download PDFInfo
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- CN105254096A CN105254096A CN201510652075.2A CN201510652075A CN105254096A CN 105254096 A CN105254096 A CN 105254096A CN 201510652075 A CN201510652075 A CN 201510652075A CN 105254096 A CN105254096 A CN 105254096A
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- water
- oil
- air flotation
- flotation pool
- gasification
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000002309 gasification Methods 0.000 title claims abstract description 34
- 238000007781 pre-processing Methods 0.000 title abstract 3
- 238000005188 flotation Methods 0.000 claims abstract description 49
- 238000005189 flocculation Methods 0.000 claims abstract description 39
- 230000016615 flocculation Effects 0.000 claims abstract description 39
- 238000005345 coagulation Methods 0.000 claims abstract description 34
- 230000015271 coagulation Effects 0.000 claims abstract description 34
- 239000000839 emulsion Substances 0.000 claims abstract description 18
- 239000000701 coagulant Substances 0.000 claims abstract description 15
- 239000010802 sludge Substances 0.000 claims abstract description 13
- 239000007787 solid Substances 0.000 claims abstract description 12
- 239000010865 sewage Substances 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 239000000084 colloidal system Substances 0.000 claims abstract description 8
- 238000011068 loading method Methods 0.000 claims abstract description 8
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 6
- 231100000719 pollutant Toxicity 0.000 claims abstract description 6
- 239000002893 slag Substances 0.000 claims abstract description 6
- 238000007667 floating Methods 0.000 claims abstract description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 40
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 claims description 40
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 24
- 239000003795 chemical substances by application Substances 0.000 claims description 21
- 230000008020 evaporation Effects 0.000 claims description 21
- 238000001704 evaporation Methods 0.000 claims description 21
- 229910021529 ammonia Inorganic materials 0.000 claims description 20
- -1 polyoxyethylene Polymers 0.000 claims description 11
- 229920006395 saturated elastomer Polymers 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 229920000642 polymer Polymers 0.000 claims description 7
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 239000007764 o/w emulsion Substances 0.000 claims description 5
- 229920003171 Poly (ethylene oxide) Polymers 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 238000012958 reprocessing Methods 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 244000144992 flock Species 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 229920001568 phenolic resin Polymers 0.000 claims description 3
- 239000005011 phenolic resin Substances 0.000 claims description 3
- 229920002401 polyacrylamide Polymers 0.000 claims description 3
- 229920001451 polypropylene glycol Polymers 0.000 claims description 3
- 230000000087 stabilizing effect Effects 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 6
- 239000008394 flocculating agent Substances 0.000 abstract 2
- 239000006247 magnetic powder Substances 0.000 abstract 2
- 239000013049 sediment Substances 0.000 abstract 2
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 230000001687 destabilization Effects 0.000 abstract 1
- 238000007790 scraping Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 14
- 239000007788 liquid Substances 0.000 description 6
- 238000013461 design Methods 0.000 description 5
- 238000002203 pretreatment Methods 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 3
- 229910000975 Carbon steel Inorganic materials 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000010962 carbon steel Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- 239000004743 Polypropylene Substances 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 150000001408 amides Chemical class 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000012937 correction Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000002641 tar oil Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Landscapes
- Physical Water Treatments (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention provides a preprocessing method for gasification ammonia-cyanide-phenol-contained circulating water. Particularly, slag scraping and oil removal are performed on gasification circulating water through advective oil separation pool, then, a coagulant, magnetic powder, an oil emulsion separated out by a flocculating agent, colloid and suspended solid sediments are added, the sediments can remove oil pollutants in water, and the magnetic powder can be recycled; coagulation, flocculation and air flotation are performed at the upper portion of a settling pond, the coagulant is added so that destabilization of the oil emulsion, the colloid and the suspended solid can be achieved, small alumen ustum is generated, the flocculating agent is added into sewage obtained after coagulation, the alumen ustum is gathered into firmer alumen ustum, flocculation water and circulating water with rich microbubbles are mixed and then enter a floatation tank, and uniform oil sludge cakes are formed on the surface of the floatation tank; processed water flows into a suction well and is recycled to an inlet of the floatation tank, and the preprocessing process of the gasification circulating water is completed. The gasification circulating water is preprocessed, the content of oil in water is decreased, and the loading coagulation oil remover and floatation technology are adopted to remove floating oil and dispersed oil in the water.
Description
Technical field
The present invention relates to a kind of circulating water for gasification pretreatment unit and pretreatment process, belong to field of water pollution control in Chemical Manufacture.
Background technology
The pretreatment technology that current synthetic ammonia industry gas making water major part adopts is: recirculated water enters gas making horizontal flow basin, by part dust tar natural subsidence, scrapes slag through the oil removing of tar oil trap, and water part internal recycling, part are sent outside.
This processing mode, circulating water for gasification water quality does not obtain basic process and improvement.And circulation causes water quality poor for a long time, cause the easy fouling of pipeline, shower nozzle easily blocks up, and it is passive to produce.Meanwhile, while environmental requirement is increased day by day, realize water correction, sewage zero-discharge is the important goal of producing.
Summary of the invention
The present invention is directed to the problems referred to above, provide a kind of combination unit loading coagulation oil removal plant and air flotation pool and pre-treatment is carried out to circulating water for gasification.Wherein, load coagulation oil removal plant to be mainly used in removing the oil slick in gas making water and thick dispersed oil; Air supporting make machinery with the fat liquor unstability of chemistry and being removed, adopt microbubble to guarantee effective air supporting.
Circulating water for gasification has different components along with the difference of feed coal, but oily substance is ubiquitous greatest problem, and oil removing is that pre-treatment is crucial.Gas making of the present invention, comprises the steps: containing the recirculated water pretreatment process of cyanogen containing phenol containing ammonia
1) circulating water for gasification is scraped after slag oil removing through advection oil separation tank, oil in water emulsion is taken off steady, coalescent by adding emulsion splitter, again dosing coagulant, magnetic, flocculation agent accelerate to separate out fat liquor, colloid and suspended solids throw out, this throw out is delivered to settling tank, by the oil pollutant removing in water, the magnetic of settling tank bottom realizes recycle by Separation and Recovery;
This technology is the object utilizing the work of additional settling agent magnetic to reach high-efficiency sedimentation and filtration in order to strengthen flocculation.Its principle in sewage, adds a small amount of coagulating agent, settling agent magnetic etc. flocculate with pollutent and be combined into one, and then filtered by High-rate sedimentation and settling agent and removed by the oil pollutant in water, settling agent magnetic realizes recycling by Separation and Recovery.
2) the water outlet gravity flow on settling tank top enters air flotation pool, coagulation, flocculation, air supporting three phases is divided in air flotation pool, in coagulation basin, dosing coagulant makes fat liquor, colloid and suspended solids de-steady, produce little alumen ustum, sewage after coagulation flows into flocculation basin, add flocculation agent in pond alumen ustum to be assembled for larger, more all even firmly alumen ustum, air flotation pool is entered after flocculation water mixes with the recirculated water being full of microbubble, alumen ustum and microbubble flock together, form uniform greasy filth cake on air flotation pool surface, then greasy filth cake is scraped into a receiving tank; Water after treatment flows in suction well, and the part water yield in suction well, by under the effect of pump, is circulated to air flotation pool entrance by dissolving;
3) through step 2) circulation after, the water outlet in air flotation pool is discharged through outlet conduit, enters vapo(u)rization system; Bed mud bottom air flotation pool sends into sludge sump, that is, complete the pretreated process of circulating water for gasification.
The described recirculated water being full of microbubble is at completing steps 2) process after, air is injected in dissolving through air compression plant, dissolve in recirculated water, then the water containing saturated air delivers to the entrance release of pressure of air flotation pool by Pressure-relief Device, this pressure-release assembly produces the bubble of 50 to 80 microns, can obtain the recirculated water being full of microbubble, this recirculated water being full of microbubble is easily attached on alumen ustum.
Described emulsion splitter is one or more in polyoxyethylene, polyoxypropylene or alkyl phenolic resin, and its addition is 50-120ppm.
Described coagulating agent is polymer alumina, and its addition is 50-120ppm.
Described flocculation agent is one or more in polyacrylamide, bodied ferric sulfate or polymerize aluminum chloride, wherein, step 1) in add-on be 1-3ppm; Step 2) in add-on be 0.5-1ppm.
The residence time of coagulation basin is 3min; The residence time in the pond of flocculation basin is 10min; The water cycle ratio of air flotation pool is 40%.
Described vapo(u)rization system is by the water outlet in air flotation pool, with 20m after namely pretreated circulating water for gasification is warming up to 60 DEG C
2the flow of/h is delivered to reboiler tube side by feeding pump and is carried out evaporation concentration, and the heating chamber course that the saturated raw steam simultaneously come by boiler enters reboiler carries out heat exchange condensation, and condensed water of condensation returns in boiler house through hot water pump again and re-uses; Circulating water for gasification is sent in flashing chamber after evaporation concentration again, and producing a large amount of secondary steams in flashing chamber after pressure control, temperature control, two secondary steam send into reprocessing in Gas-making Furnace through flashing chamber top after overheated, voltage stabilizing.
The pressure of raw steam controls as 0.618MPa, and raw vapor temperature controls to be 160 DEG C; The circulating water for gasification steam output sent into again after evaporation concentration in flashing chamber controls as 19800kg/h; Two secondary steam pressures control as 0.199MPa, and two secondary vapor temperatures control to be 120 DEG C; In flashing chamber, liquidus temperature controls is 125 DEG C, and wherein, the effective temperature difference of liquid phase and gas phase controls to be 34 DEG C; Flashing chamber overhead vapor pressure-controlling is 0.199MPa, and flashing chamber inner top controls as 17680m to the secondary steam amount of Gas-making Furnace
3/ h.
The present invention also provide a kind of gas making containing ammonia containing cyanogen containing the recirculated water pretreatment process of phenol treatment unit used, this pretreatment unit comprises loading coagulation oil removal plant, air-floating apparatus and evaporation unit, wherein, load coagulation oil removal plant and comprise mixing pit, the dosing pond of emulsion splitter, flocculation basin, settling tank; Settling tank top is connected with air flotation pool device through carrier pipe, is connected bottom settling tank after pipeline is connected with pump with magnetic withdrawing can again, magnetic withdrawing can again with sludge dehydration device; Air flotation pool device comprises coagulation basin and flocculation basin, and be connected through the bottom of carrier pipe with the carrier pipe in the middle of air flotation pool bottom flocculation basin, air flotation pool upper end is provided with outlet conduit, and bottom air flotation pool and bottom is also provided with the pipeline to sludge sump.
Described evaporation unit comprises reboiler, flashing chamber, and saturated raw steam is connected with reboiler top through carrier pipe, and parallel connection passes to heating chamber shell side and connects; Pretreated circulating water for gasification is connected parallel connection through carrier pipe with the bottom of reboiler and passes to reboiler tube side; Reboiler top is connected with flashing chamber through carrier pipe, and flashing chamber top is connected to Gas-making Furnace through carrier pipe; After carrier pipe converges, feed reservoir is connected to bottom flashing chamber with bottom reboiler; Reboiler bottom is connected to boiler house through carrier pipe.
After device of the present invention puts into operation, circulating water for gasification is through pre-treatment, reduce the content (oil-in-water mainly exists with oil in water emulsion form, the oil slick that surfactant suspension is a small amount of) of oil-in-water, adopt loading coagulation oil eliminator and air-float technology to be mainly used in removing the oil slick in water and dispersed oil.
Accompanying drawing explanation
Fig. 1 is for loading coagulation oil removal plant structural representation.
Fig. 2 is air-floating apparatus structural representation.
Fig. 3 is evaporation unit
Embodiment
Embodiment 1
After the present invention takes to scrape SS in slag, breakdown of emulsion precipitation, pneumatically supported pretreatment process removing circulating water for gasification, oil slick, oil in water emulsion, the remaining material such as ammonia, cyanogen, phenol enters vapo(u)rization system with aqueous phase, ammonia, cyanogen, phenol etc. to be brought in steam by malleation evaporation and enter gasification system as vaporization agent, ammonia, cyanogen, phenol etc. sinter and reduce in Gas-making Furnace.The method using containing ammonia containing cyanogen containing the circulating water for gasification of phenol send into after pre-treatment vapo(u)rization system produce steam, after send into gasification system as vaporization agent, eliminate objectionable impurities ammonia, cyanogen and the phenol etc. that contain in circulating water for gasification, reduce the deterioration to system process links such as gas making cooling, washings that objectionable impurities causes in the circulation of gasification system.
Gas making containing ammonia containing cyanogen containing the recirculated water pretreatment process of phenol treatment unit used, this energy sewage pre-treatment device comprises loading coagulation oil removal plant, air-floating apparatus and evaporation unit, wherein, loads coagulation oil removal plant and comprises mixing pit, the dosing pond of emulsion splitter, flocculation basin, settling tank.
Settling tank top is connected with air flotation pool device through carrier pipe, is connected bottom settling tank after pipeline is connected with pump with magnetic withdrawing can again, magnetic withdrawing can again with sludge dehydration device.
Air flotation pool device comprises coagulation basin and flocculation basin, and be connected through the bottom of carrier pipe with the carrier pipe in the middle of air flotation pool bottom flocculation basin, air flotation pool upper end is provided with outlet conduit, and bottom air flotation pool and bottom is also provided with the pipeline to sludge sump.
Evaporation unit comprises reboiler, flashing chamber, and saturated raw steam is connected with reboiler top through carrier pipe, and parallel connection passes to heating chamber shell side and connects; Pretreated circulating water for gasification is connected parallel connection through carrier pipe with the bottom of reboiler and passes to reboiler tube side; Reboiler top is connected with flashing chamber through carrier pipe, and flashing chamber top is connected to Gas-making Furnace through carrier pipe; After carrier pipe converges, feed reservoir is connected to bottom flashing chamber with bottom reboiler; Reboiler bottom is connected to boiler house through carrier pipe.
Embodiment 2
A kind of typical gas making sewage COD:8000 ~ 10000mg/L; Ammonia nitrogen: 2000 ~ 3000mg/L; Phenol: 1000 ~ 1100mg/L; Cyanogen: 0.8 ~ 1.1mg/L; PH: weakly alkaline; Water temperature: 60 ~ 80 DEG C.
Perform above-mentioned pretreatment process, comprise the steps:
1) circulating water for gasification and energy sewage are scraped after slag oil removing through advection oil separation tank, oil in water emulsion is taken off steady, coalescent by adding emulsion splitter, again dosing coagulant, magnetic, flocculation agent accelerate to separate out fat liquor, colloid and suspended solids throw out, this throw out is delivered to settling tank, by the oil pollutant removing in water, the magnetic of settling tank bottom realizes recycle by Separation and Recovery.
This technology is the object utilizing the work of additional settling agent magnetic to reach high-efficiency sedimentation and filtration in order to strengthen flocculation.Its principle in sewage, adds a small amount of coagulating agent, settling agent magnetic etc. flocculate with pollutent and be combined into one, and then filtered by High-rate sedimentation and settling agent and removed by the oil pollutant in water, settling agent magnetic realizes recycling by Separation and Recovery.
Mixing pit in this programme is divided into emulsion splitter dosing pond, coagulation basin, loading coagulation basin, flocculation basin.Wherein emulsion splitter adds in pond and adds emulsion splitter, destroys emulsus oil, solid phase is assembled, be convenient to the removal of oil.
2) the water outlet gravity flow on settling tank top enters air flotation pool, coagulation, flocculation, air supporting three phases is divided in air flotation pool, in coagulation basin, dosing coagulant makes fat liquor, colloid and suspended solids de-steady, produce little alumen ustum, sewage after coagulation flows into flocculation basin, add flocculation agent in pond alumen ustum to be assembled for larger, more all even firmly alumen ustum, air flotation pool is entered after flocculation water mixes with the recirculated water being full of microbubble, alumen ustum and microbubble flock together, form uniform greasy filth cake on air flotation pool surface, then greasy filth cake is scraped into a receiving tank; Water after treatment flows in suction well, and the part water yield in suction well, by under the effect of pump, is circulated to air flotation pool entrance by dissolving.
3) through step 2) circulation after, the water outlet in air flotation pool is discharged through outlet conduit, and the water of discharge enters vapo(u)rization system; Bed mud bottom air flotation pool sends into sludge sump, that is, complete the pretreated process of circulating water for gasification.
The described recirculated water being full of microbubble is at completing steps 2) process after, air is injected in dissolving through air compression plant, dissolve in recirculated water, then the water containing saturated air delivers to the entrance release of pressure of air flotation pool by Pressure-relief Device, this pressure-release assembly produces the bubble of 50 to 80 microns, can obtain the recirculated water being full of microbubble, this recirculated water being full of microbubble is easily attached on alumen ustum.
Described emulsion splitter is one or more in polyoxyethylene, polyoxypropylene or alkyl phenolic resin, and its addition is 50-120ppm.
Described coagulating agent is polymer alumina, and its addition is 50-120ppm.
Described flocculation agent is one or more in polyacrylamide, bodied ferric sulfate or polymerize aluminum chloride, wherein, step 1) in add-on be 1-3ppm; Step 2) in add-on be 0.5-1ppm.
The present invention's its parameter in actual moving process is as follows:
| Parameter | Unit | Design load |
| Coagulation basin | Seat | 2 |
| Single pond residence time | min | 3 |
| Single pond useful volume | m 3 | 1 |
| Parameter | Unit | Design load |
| Flocculation basin | Seat | 2 |
| Single pond residence time | min | 10 |
| Single pond useful volume | m 3 | 3.5 |
| Parameter | Unit | Design load |
| Air flotation pool | Seat | 2 |
| Effective diameter | m | 3 |
| Water cycle ratio | m | 40％ |
In medicine system
Coagulating agent
Design adopts solid PAC as coagulating agent.Be added in corresponding process pool by dosing pump after being configured to liquid by configured pool.
Load coagulation oil eliminator dosage: 100mg/l, with pure Al
2o
3meter.
Unibub
tMair flotation pool dosage: 100mg/l, with pure Al
2o
3meter.
Flocculation agent
Adopt solid polypropylene acid amides as flocculation agent.In dosing, the polymer preparing apparatus installing automatization adds dissolution of solid polymer to be become the liquid polymers of 2g/l.Be added to after liquid polymers on-line dilution to 0.1 ~ 0.2g/L again in water.Adopt 90% pure solid powder.
Load coagulation oil eliminator flocculation basin dosage: 2mg/l.
Unibub
tMair supporting flocculation basin dosage: 1mg/l.
Emulsion splitter
Employing polyoxyethylene is emulsion splitter, loads coagulation oil eliminator emulsion splitter dosage: 100mg/l.
Magnetic
Magnetic adds and adds for disposable, follow-up regularly a small amount of replenish loss amount, the magnetic rate of recovery 90% ~ 95%.
Sludge yield
Mud main source:
Load coagulation oil eliminator and produce mud;
Unibub
tMthe bed mud of air flotation pool and scum silica frost;
Sludge output: 310DSkg/d
Because mud amount is less, not independent set handling system, unifies sludge treating system by place and processes.
Design effluent quality: SS≤30mg/L, non-solubility oil≤100mg/L.
Embodiment 3
Water outlet in embodiment 2 in air flotation pool, with 20m after namely pretreated circulating water for gasification is warming up to 60 DEG C
2the flow of/h is delivered to reboiler tube side by feeding pump and is carried out evaporation concentration, and the heating chamber course that the saturated raw steam simultaneously come by boiler enters reboiler carries out heat exchange condensation, and condensed water of condensation returns in boiler house through hot water pump again and re-uses; Circulating water for gasification is sent in flashing chamber after evaporation concentration again, and producing a large amount of secondary steams in flashing chamber after pressure control, temperature control, two secondary steam send into reprocessing in Gas-making Furnace through flashing chamber top after overheated, voltage stabilizing.This process device used is evaporation unit, and the treatment capacity of its evaporation unit is 20m
3/ h, the quality parameter of water outlet in air supporting: composition: SS<30mg/L; Oil: naked eyes are not seen; Phenol: 700 ~ 1000mg/L; Specific conductivity: 25 μ S/cm; Salinity: 1%; Raw material proportion: 1000kg/m
3; PH value: 8 ~ 9; Treatment capacity: 20m
3/ h.
Reboiler two (carbon steel, a titanium material), flashing chamber carbon steel.
Have a small amount of salt in evaporative process to analyze, need regular extraction reprocessing.
In this process, the pressure of raw steam controls as 0.618MPa, and raw vapor temperature controls to be 160 DEG C; The circulating water for gasification steam output sent into again after evaporation concentration in flashing chamber controls as 19800kg/h; Two secondary steam pressures control as 0.199MPa, and two secondary vapor temperatures control to be 120 DEG C; In flashing chamber, liquidus temperature controls is 125 DEG C, and wherein, the effective temperature difference of liquid phase and gas phase controls to be 34 DEG C; Flashing chamber overhead vapor pressure-controlling is 0.199MPa, and flashing chamber inner top controls as 17680m to the secondary steam amount of Gas-making Furnace
3/ h.
A small amount of non-condensable gas can be produced in native system, long term accumulation can be partially formed higher concentration in condensation side, heat transfer efficiency is caused obviously to decline, so be provided with special noncondensable gas relief outlet at reboiler heating chamber, in evaporative process, open non-condensable gas valve at any time regularly discharge, to improve heat transfer efficiency.
For feed liquid physical property and evaporation object, requirement, natural-circulation evaporator selected by vaporizer, natural-circulation evaporator in evaporative process, feed liquid enter oven heats heat up, owing to not reaching the temperature of saturation under this state, solution does not seethe with excitement.Along with heating and the reduction of intraductal pressure, when after the saturated pressure under the temperature of solution reaches this state, come to life, thus produce a large amount of bubble, the density of solution also reduces thereupon, the density difference existed between the feed liquid of the not boiling of the liquid-vapor mixture like this in boiling tube and circulation tube side, defines the circulation impellent of external-heat natural-circulation evaporator.In order to prevent fouling and partial crystallization, heating tube should operate under complete submerged state.This vaporizer is applicable to the evaporation concentration of the not serious and less solution of corrodibility of fouling, and its advantage is that structure is simple, and be convenient to manufacture, power consumption is low.The energy consumption produced in this process is: system throughput: 20m
3/ h; System steam output: 19.8t/h; Steam consumption: 26.1t/h; Installed power: 16.5kw.
Claims (10)
1. gas making is containing ammonia containing the recirculated water pretreatment process of cyanogen containing phenol, it is characterized in that, comprises the steps:
Circulating water for gasification is scraped after slag oil removing through advection oil separation tank, oil in water emulsion is taken off steady, coalescent by adding emulsion splitter, again dosing coagulant, magnetic, flocculation agent accelerate to separate out fat liquor, colloid and suspended solids throw out, this throw out is delivered to settling tank, by the oil pollutant removing in water, the magnetic of settling tank bottom realizes recycle by Separation and Recovery;
The water outlet gravity flow on settling tank top enters air flotation pool, coagulation, flocculation, air supporting three phases is divided in air flotation pool, in coagulation basin, dosing coagulant makes fat liquor, colloid and suspended solids de-steady, produce little alumen ustum, sewage after coagulation flows into flocculation basin, add flocculation agent in pond alumen ustum to be assembled for larger, more all even firmly alumen ustum, air flotation pool is entered after flocculation water mixes with the recirculated water being full of microbubble, alumen ustum and microbubble flock together, form uniform greasy filth cake on air flotation pool surface, then greasy filth cake is scraped into a receiving tank; Water after treatment flows in suction well, and the part water yield in suction well, by under the effect of pump, is circulated to air flotation pool entrance by dissolving;
Through step 2) circulation after, the water outlet in air flotation pool is discharged through outlet conduit, enters vapo(u)rization system; Bed mud bottom air flotation pool sends into sludge sump, that is, complete the pretreated process of circulating water for gasification.
2. gas making according to claim 1 contains the recirculated water pretreatment process of phenol containing cyanogen containing ammonia, it is characterized in that, the described recirculated water being full of microbubble is at completing steps 2) process after, air is injected in dissolving through air compression plant, dissolve in recirculated water, then the water containing saturated air delivers to the entrance release of pressure of air flotation pool by Pressure-relief Device, this pressure-release assembly produces the bubble of 50 to 80 microns, can obtain the recirculated water being full of microbubble, this recirculated water being full of microbubble is easily attached on alumen ustum.
3. gas making according to claim 1 containing ammonia containing cyanogen containing the recirculated water pretreatment process of phenol, it is characterized in that, described emulsion splitter is one or more in polyoxyethylene, polyoxypropylene or alkyl phenolic resin, and its addition is 50-120ppm.
4. gas making according to claim 1 is containing ammonia containing the recirculated water pretreatment process of cyanogen containing phenol, and it is characterized in that, described coagulating agent is polymer alumina, and its addition is 50-120ppm.
5. gas making according to claim 1 contains the recirculated water pretreatment process of phenol containing cyanogen containing ammonia, it is characterized in that, described flocculation agent is one or more in polyacrylamide, bodied ferric sulfate or polymerize aluminum chloride, wherein, step 1) in add-on be 1-3ppm; Step 2) in add-on be 0.5-1ppm.
6. gas making according to claim 1 is containing ammonia containing the recirculated water pretreatment process of cyanogen containing phenol, and it is characterized in that, the residence time of coagulation basin is 3min; The residence time in the pond of flocculation basin is 10min; The water cycle ratio of air flotation pool is 40%.
7. gas making according to claim 1 contains the recirculated water pretreatment process of phenol containing cyanogen containing ammonia, it is characterized in that, described vapo(u)rization system is by the water outlet in air flotation pool, namely deliver to reboiler tube side with the flow of 20 ㎡/h by feeding pump after pretreated circulating water for gasification is warming up to 60 DEG C and carry out evaporation concentration, the heating chamber course that the saturated raw steam simultaneously come by boiler enters reboiler carries out heat exchange condensation, and condensed water of condensation returns in boiler house through hot water pump again and re-uses; Circulating water for gasification is sent in flashing chamber after evaporation concentration again, and producing a large amount of secondary steams in flashing chamber after pressure control, temperature control, two secondary steam send into reprocessing in Gas-making Furnace through flashing chamber top after overheated, voltage stabilizing.
8. gas making according to claim 7 is containing ammonia containing the recirculated water pretreatment process of cyanogen containing phenol, it is characterized in that, the pressure of raw steam controls as 0.618MPa, and raw vapor temperature controls to be 160 DEG C; The circulating water for gasification steam output sent into again after evaporation concentration in flashing chamber controls as 19800kg/h; Two secondary steam pressures control as 0.199MPa, and two secondary vapor temperatures control to be 120 DEG C; In flashing chamber, liquidus temperature controls is 125 DEG C, and wherein, the effective temperature difference of liquid phase and gas phase controls to be 34 DEG C; Flashing chamber overhead vapor pressure-controlling is 0.199MPa, and flashing chamber inner top controls as 17680m to the secondary steam amount of Gas-making Furnace
3/ h.
9. the gas making described in any one of claim 1-8 containing ammonia containing cyanogen containing the recirculated water pretreatment process of phenol treatment unit used, it is characterized in that, this pretreatment unit comprises loading coagulation oil removal plant, air-floating apparatus and evaporation unit, wherein, load coagulation oil removal plant and comprise mixing pit, the dosing pond of emulsion splitter, flocculation basin, settling tank; Settling tank top is connected with air flotation pool device through carrier pipe, is connected bottom settling tank after pipeline is connected with pump with magnetic withdrawing can again, magnetic withdrawing can again with sludge dehydration device; Air flotation pool device comprises coagulation basin and flocculation basin, and be connected through the bottom of carrier pipe with the carrier pipe in the middle of air flotation pool bottom flocculation basin, air flotation pool upper end is provided with outlet conduit, and bottom air flotation pool and bottom is also provided with the pipeline to sludge sump.
10. gas making according to claim 9 contains the recirculated water pretreatment unit of phenol containing cyanogen containing ammonia, it is characterized in that, described evaporation unit comprises reboiler, flashing chamber, and saturated raw steam is connected with reboiler top through carrier pipe, and parallel connection passes to heating chamber shell side and connects; Pretreated circulating water for gasification is connected parallel connection through carrier pipe with the bottom of reboiler and passes to reboiler tube side; Reboiler top is connected with flashing chamber through carrier pipe, and flashing chamber top is connected to Gas-making Furnace through carrier pipe; After carrier pipe converges, feed reservoir is connected to bottom flashing chamber with bottom reboiler; Reboiler bottom is connected to boiler house through carrier pipe.
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| CN111285506A (en) * | 2020-03-30 | 2020-06-16 | 无锡市政设计研究院有限公司 | Pretreatment system and pretreatment method for wastewater membrane treatment process |
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| RU2696711C1 (en) * | 2018-06-18 | 2019-08-05 | Борис Семенович Ксенофонтов | Method of waste water treatment |
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