CN105254096B - A kind of gas making is containing ammonia containing circulation water pretreatment process and device of the cyanogen containing phenol - Google Patents

A kind of gas making is containing ammonia containing circulation water pretreatment process and device of the cyanogen containing phenol Download PDF

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CN105254096B
CN105254096B CN201510652075.2A CN201510652075A CN105254096B CN 105254096 B CN105254096 B CN 105254096B CN 201510652075 A CN201510652075 A CN 201510652075A CN 105254096 B CN105254096 B CN 105254096B
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water
flotation tank
oil
gasification
cyanogen
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CN105254096A (en
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蒋远华
杨晓勤
卢钢
张战利
黄登兵
朱洪波
李天方
冯加新
杨晓华
黄志亮
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XINJIANG YIHUA CHEMICAL CO Ltd
YIHUA GROUP CO Ltd HUBEI PROV
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XINJIANG YIHUA CHEMICAL CO Ltd
YIHUA GROUP CO Ltd HUBEI PROV
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Abstract

The present invention provides a kind of gas making containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, specifically by circulating water for gasification after advection oil separation tank scrapes slag oil removing, through demulsification coalescence, again plus coagulant, magnetic, flocculant separate out fat liquor, colloid and suspended solid sediment, the sediment removes the oil pollutant in water, and magnetic is recycled.The water outlet of sedimentation basin top is through coagulation, flocculation, air supporting three phases, make fat liquor, colloid and suspended solid de- steady through dosing coagulant, produce small alumen ustum, sewage after coagulation adds flocculant that alumen ustum is collected as into stronger alumen ustum, flocculation water enters flotation tank with being full of after the recirculated water of microbubble is mixed, and uniform greasy filth cake is formed in air supporting pool surface;Water after treatment, which is flowed into, is recycled to flotation tank entrance in absorbing well, absorption well, complete circulating water for gasification preprocessing process.Circulating water for gasification is preprocessed, and oily content, the oil slick and dispersed oil in water are eliminated using loading coagulation oil expeller and air-float technology in reduction water.

Description

A kind of gas making is containing ammonia containing circulation water pretreatment process and device of the cyanogen containing phenol
Technical field
The present invention relates to a kind of circulating water for gasification pretreatment unit and preprocess method, belong to water pollution control in Chemical Manufacture Field processed.
Background technology
The pretreating process that synthesis ammonia industry gas making water is largely used at present for:Recirculated water enters gas making horizontal flow basin, will Part dust tar natural subsidence, scrape slag through tar oil interceptor oil removing, water part inner loop, partly send outside.
The processing mode, circulating water for gasification water quality does not obtain basic processing and improvement.And prolonged circulation is caused Water quality is poor, causes the easy fouling of pipeline, and shower nozzle is easily blocked up, and production is passive.Meanwhile, while environmental requirement is increasingly increased, realize Water correction, sewage zero-discharge are the important goals of production.
The content of the invention
The present invention is regarding to the issue above there is provided a kind of combination unit for loading coagulation degreasing unit and flotation tank to gas making Recirculated water is pre-processed.Wherein, loading coagulation degreasing unit is mainly used in removing the oil slick and coarse dispersion oil in gas making water;Gas It is floating to make machinery and chemistry fat liquor unstability and be removed, microbubble is used to ensure effective air supporting.
Circulating water for gasification has a different components with the difference of feed coal, but oily substance is that the maximum of generally existing is asked Topic, oil removing is crucial for pretreatment.Gas making of the present invention, containing circulation water pretreatment process of the cyanogen containing phenol, comprises the following steps containing ammonia:
1) circulating water for gasification is after advection oil separation tank scrapes slag oil removing, by adding demulsifier by the de- steady, coalescence of oil emulsion, Dosing coagulant, magnetic, flocculant accelerate fat liquor, colloid and the suspended solid sediment separated out again, and the sediment is delivered to Sedimentation basin, the oil pollutant in water is removed, and the magnetic of sedimentation basin bottom is recycled by separating and recovering realization;
This technology is to reach high-efficiency sedimentation and the purpose filtered using the effect of additional settling agent magnetic to strengthen flocculation. Its principle is to add a small amount of coagulant, settling agent magnetic etc. into sewage to be combined into one with pollutant flocculation, then passes through height Effect precipitation is filtered with settling agent removes the oil pollutant in water, and settling agent magnetic realizes recycling by separating and recovering.
2) the water outlet gravity flow on sedimentation basin top, which enters, is divided into coagulation, flocculation, air supporting three phases in flotation tank, flotation tank, Into coagulating basin, dosing coagulant makes fat liquor, colloid and suspended solid de- steady, produces the sewage after small alumen ustum, coagulation and flows into wadding Added in solidifying pond, pond flocculant by alumen ustum be collected as it is larger, be more uniformly distributed and firm alumen ustum, flocculation water and be full of microbubble Recirculated water mixing after enter flotation tank, alumen ustum flocked together with microbubble, and uniform greasy filth cake is formed in air supporting pool surface, Then greasy filth cake is scraped into a collecting tank;Water after treatment is flowed into absorbing well, absorption well, and the part water in absorbing well, absorption well will be In the presence of pump, flotation tank entrance is recycled to by dissolving;
3) through step 2) circulation after, the water outlet in flotation tank is discharged through outlet conduit, into vapo(u)rization system;Flotation tank bottom The bed mud feeding sludge-tank in portion, i.e. complete the process of circulating water for gasification pretreatment.
The described recirculated water of microbubble that is full of is to complete step 2) process after, air is noted through air compression plant Enter in dissolving, dissolved in recirculated water, then the water containing saturated air delivers to the entrance of flotation tank by pressure relief device Release of pressure, the pressure-release assembly produces 50 to 80 microns of bubble, you can obtain being full of the recirculated water of microbubble, this is full of microbubble Recirculated water is easily attached on alumen ustum.
Described demulsifier is the one or more in polyoxyethylene, polyoxypropylene or alkyl phenolic resin, its addition For 50-120ppm.
Described coagulant is polymer alumina, and its addition is 50-120ppm.
Described flocculant is the one or more in polyacrylamide, bodied ferric sulfate or aluminium polychloride, wherein, step It is rapid 1) in addition be 1-3ppm;Step 2) in addition be 0.5-1ppm.
The residence time of coagulating basin is 3min;The residence time in the pond of flocculation basin is 10min;The water circulation ratio of flotation tank is 40%.
Described vapo(u)rization system be by the water outlet in flotation tank, i.e., pretreated circulating water for gasification be warming up to after 60 DEG C with 20m2/ h flow is pumped to reboiler tube side by feeding and is evaporated concentration, at the same by boiler Lai saturation life steam enter again The heating chamber course for boiling device carries out heat exchange condensation, and condensed condensed water is returned again in boiler room through heat-exchanger pump and re-used;Make Gas recirculated water is re-fed into flash chamber after evaporation and concentration, produces substantial amounts of indirect steam after pressure control, temperature control in flash chamber, Two secondary steam are after overheat, voltage stabilizing through being reprocessed at the top of flash chamber in feeding Gas-making Furnace.
The pressure control of raw steam is 0.618MPa, and raw vapor (steam) temperature control is 160 DEG C;Circulating water for gasification is through being concentrated by evaporation The evaporation capacity control being re-fed into afterwards in flash chamber is 19800kg/h;Two secondary steam pressure controls are 0.199MPa, two secondary steamings Stripping temperature control is 120 DEG C;Liquidus temperature control is 125 DEG C in flash chamber, wherein, the effective temperature difference control of liquid phase and gas phase is 34℃;Flash chamber overhead vapor Stress control is 0.199MPa, and the indirect steam amount control of flash distillation indoor top to Gas-making Furnace is 17680m3/h。
The present invention also provides a kind of gas making containing ammonia containing the processing unit used by circulation water pretreatment process of the cyanogen containing phenol, and this is pre- Processing unit includes loading coagulation degreasing unit, air-floating apparatus and vaporising device, wherein, loading coagulation degreasing unit includes mixing Pond, the dosing pond of demulsifier, flocculation basin, sedimentation basin;Sedimentation basin top is connected through conveying pipeline with air supporting pool device, sedimentation basin bottom Be connected again with magnetic recycling can after being connected through pipeline with pump, magnetic recycling can again with sludge dehydration device;Air supporting pool device includes Coagulating basin and flocculation basin, bottom connection of the flocculation basin bottom through the conveying pipeline in the middle of conveying pipeline and flotation tank, flotation tank upper end is set Outlet conduit is equipped with, flotation tank bottom and bottom are additionally provided with to the pipeline of sludge-tank.
Described vaporising device includes reboiler, flash chamber, and saturation life steam is connected through conveying pipeline with reboiler top, and UNICOM to heating chamber shell side is connected;Pretreated circulating water for gasification is passed to again through conveying pipeline is in parallel with the bottom connection of reboiler Boil device tube side;It is connected at the top of reboiler through conveying pipeline with flash chamber, Gas-making Furnace is connected to through conveying pipeline at the top of flash chamber;Flash chamber Bottom is connected to feed reservoir after converging with reboiler bottom through conveying pipeline;Reboiler bottom is connected to boiler room through conveying pipeline.
After device of the present invention puts into operation, circulating water for gasification is preprocessed, oily content in reduction water (in water oil it is main with Emulsify oil form to exist, a small amount of oil slick of surfactant suspension), water removal is mainly used in using loading coagulation oil expeller and air-float technology In oil slick and dispersed oil.
Brief description of the drawings
Fig. 1 is loading coagulation degreasing unit structural representation.
Fig. 2 is air-floating apparatus structural representation.
Fig. 3 is vaporising device
Embodiment
Embodiment 1
The present invention, which takes, scrapes slag, demulsification precipitation, the SS in pneumatically supported preprocess method removing circulating water for gasification, oil slick, breast After carburetion, the material such as remaining ammonia, cyanogen, phenol enters vapo(u)rization system with aqueous phase, and into the steaming is brought such as ammonia, cyanogen, phenol by malleation evaporation Enter gasification system in vapour as vaporization agent, ammonia, cyanogen, phenol etc. are sintered and reduced in Gas-making Furnace.This method will contain ammonia and contain containing cyanogen The circulating water for gasification of phenol sent into after pretreatment vapo(u)rization system produce steam, after feeding gasification system as vaporization agent, remove Harmful substance ammonia, cyanogen and phenol contained in circulating water for gasification etc., reduces harmful substance right caused by the circulation of gasification system The deterioration of the system process links such as gas making cooling, washing.
Gas making is containing ammonia containing the processing unit used by circulation water pretreatment process of the cyanogen containing phenol, the energy sewage pre-treatment device Including loading coagulation degreasing unit, air-floating apparatus and vaporising device, wherein, loading coagulation degreasing unit includes mixing pit, demulsification The dosing pond of agent, flocculation basin, sedimentation basin.
Sedimentation basin top is connected through conveying pipeline with air supporting pool device, sedimentation basin bottom be connected through pipeline with pump after again with magnetic Recycling can connect, magnetic recycling can again with sludge dehydration device.
Air supporting pool device includes coagulating basin and flocculation basin, and flocculation basin bottom is through the conveying pipeline in the middle of conveying pipeline and flotation tank Bottom is connected, and flotation tank upper end is provided with outlet conduit, and flotation tank bottom and bottom are additionally provided with to the pipeline of sludge-tank.
Vaporising device includes reboiler, flash chamber, and saturation life steam is connected through conveying pipeline with reboiler top, and parallel connection is passed to Heating chamber shell side is connected;Pretreated circulating water for gasification passes to reboiler pipe through conveying pipeline is in parallel with the bottom connection of reboiler Journey;It is connected at the top of reboiler through conveying pipeline with flash chamber, Gas-making Furnace is connected to through conveying pipeline at the top of flash chamber;Flash chamber bottom with Reboiler bottom is connected to feed reservoir after converging through conveying pipeline;Reboiler bottom is connected to boiler room through conveying pipeline.
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:Alkalescent;Water temperature:60~80 DEG C.
Above-mentioned preprocess method is performed, is comprised the following steps:
1) circulating water for gasification be energy sewage after advection oil separation tank scrapes slag oil removing, by adding demulsifier by oil emulsion De- steady, coalescence, then dosing coagulant, magnetic, flocculant accelerate fat liquor, colloid and the suspended solid sediment of precipitation, and this sinks Starch is delivered to sedimentation basin, and the oil pollutant in water is removed, and the magnetic of sedimentation basin bottom realizes circulation by separating and recovering Utilize.
This technology is to reach high-efficiency sedimentation and the purpose filtered using the effect of additional settling agent magnetic to strengthen flocculation. Its principle is to add a small amount of coagulant, settling agent magnetic etc. into sewage to be combined into one with pollutant flocculation, then passes through height Effect precipitation is filtered with settling agent removes the oil pollutant in water, and settling agent magnetic realizes recycling by separating and recovering.
Mixing pit in this programme is divided into demulsifier dosing pond, coagulating basin, loading coagulating basin, flocculation basin.Wherein demulsifier Add in pond plus demulsifier, destruction emulsus oil assembles solid phase, is easy to the removal of oil.
2) the water outlet gravity flow on sedimentation basin top, which enters, is divided into coagulation, flocculation, air supporting three phases in flotation tank, flotation tank, Into coagulating basin, dosing coagulant makes fat liquor, colloid and suspended solid de- steady, produces the sewage after small alumen ustum, coagulation and flows into wadding Added in solidifying pond, pond flocculant by alumen ustum be collected as it is larger, be more uniformly distributed and firm alumen ustum, flocculation water and be full of microbubble Recirculated water mixing after enter flotation tank, alumen ustum flocked together with microbubble, and uniform greasy filth cake is formed in air supporting pool surface, Then greasy filth cake is scraped into a collecting tank;Water after treatment is flowed into absorbing well, absorption well, and the part water in absorbing well, absorption well will be In the presence of pump, flotation tank entrance is recycled to by dissolving.
3) through step 2) circulation after, the water outlet in flotation tank is discharged through outlet conduit, and the water of discharge enters vapo(u)rization system; The bed mud feeding sludge-tank of flotation tank bottom, i.e. complete the process of circulating water for gasification pretreatment.
The described recirculated water of microbubble that is full of is to complete step 2) process after, air is noted through air compression plant Enter in dissolving, dissolved in recirculated water, then the water containing saturated air delivers to the entrance of flotation tank by pressure relief device Release of pressure, the pressure-release assembly produces 50 to 80 microns of bubble, you can obtain being full of the recirculated water of microbubble, this is full of microbubble Recirculated water is easily attached on alumen ustum.
Described demulsifier is the one or more in polyoxyethylene, polyoxypropylene or alkyl phenolic resin, its addition For 50-120ppm.
Described coagulant is polymer alumina, and its addition is 50-120ppm.
Described flocculant is the one or more in polyacrylamide, bodied ferric sulfate or aluminium polychloride, wherein, step It is rapid 1) in addition be 1-3ppm;Step 2) in addition be 0.5-1ppm.
The present invention its parameter in actual moving process is as follows:
Parameter Unit Design load
Coagulating basin Seat 2
Single pond residence time min 3
Single pond dischargeable capacity m3 1
Parameter Unit Design load
Flocculation basin Seat 2
Single pond residence time min 10
Single pond dischargeable capacity m3 3.5
Parameter Unit Design load
Flotation tank Seat 2
Effective diameter m 3
Water circulation ratio m 40%
In medicine system
Coagulant
Design is used as coagulant using solid PAC.It is configured to after liquid be added to accordingly by dosing pump by configured pool Process pool in.
Load coagulation oil expeller dosage:100mg/l, with pure Al2O3Meter.
UnibubTMFlotation tank dosage:100mg/l, with pure Al2O3Meter.
Flocculant
Flocculant is used as using solid polypropylene acid amides.In the dosing, install the polymer preparing apparatus of automation with Dissolution of solid polymer is added into 2g/l liquid polymers.By liquid polymers on-line dilution to 0.1~0.2g/L It is added to again in water afterwards.Using 90% pure solid powder.
Load coagulation oil expeller flocculation basin dosage:2mg/l.
UnibubTMAir supporting flocculation basin dosage:1mg/l.
Demulsifier
Polyoxyethylene is used for demulsifier, coagulation oil expeller demulsifier dosage is loaded:100mg/l.
Magnetic
Magnetic is added disposably to add, follow-up periodically a small amount of supplement loss amount, the magnetic rate of recovery 90%~95%.
Sludge yield
Sludge main source:
Load coagulation oil expeller production mud;
UnibubTMThe bed mud and scum silica frost of flotation tank;
Sludge output:310DS kg/d
Because mud amount is smaller, processing system is not separately provided, unifying sludge treating system by place is handled.
Design effluent quality:SS≤30mg/L, non-solubility oil≤100mg/L.
Embodiment 3
Water outlet in embodiment 2 in flotation tank, i.e., pretreated circulating water for gasification is warming up to after 60 DEG C with 20m2/ h's Flow is pumped to reboiler tube side by feeding and is evaporated concentration, at the same by boiler Lai saturation life steam enter reboiler plus Hot cell course carries out heat exchange condensation, and condensed condensed water is returned again in boiler room through heat-exchanger pump and re-used;Circulating water for gasification It is re-fed into after evaporation and concentration in flash chamber, produces substantial amounts of indirect steam, two secondary steamings after pressure control, temperature control in flash chamber Vapour is after overheat, voltage stabilizing through being reprocessed at the top of flash chamber in feeding Gas-making Furnace.Device used by the process is vaporising device, and it steams The treating capacity of transmitting apparatus is 20m3The water quality parameter of water outlet in/h, air supporting:Composition:SS<30mg/L;Oil:Naked eyes are not seen; Phenol:700~1000mg/L;Electrical conductivity:25μS/cm;Salinity:1%;Raw material proportion:1000kg/m3;PH value:8~9;Treating capacity: 20m3/h。
Reboiler two (carbon steel, a titanium), flash chamber carbon steel.
A small amount of salt is had in evaporation process to analyze, and need to periodically produce reprocessing.
During being somebody's turn to do, the pressure control of raw steam is 0.618MPa, and raw vapor (steam) temperature controls to be 160 DEG C;Circulating water for gasification The evaporation capacity control being re-fed into after evaporation and concentration in flash chamber is 19800kg/h;Two secondary steam pressures are controlled 0.199MPa, two secondary vapor (steam) temperature controls are 120 DEG C;Liquidus temperature control is 125 DEG C in flash chamber, wherein, liquid phase and gas The effective temperature difference control of phase is 34 DEG C;Flash chamber overhead vapor Stress control is 0.199MPa, flash distillation indoor top to Gas-making Furnace Indirect steam amount control be 17680m3/h。
A small amount of fixed gas can be produced in the system, long term accumulation can be partially formed higher concentration in condensation side, cause Heat transfer efficiency is decreased obviously, so being provided with special on-condensible gas outlet in reboiler heating chamber, in evaporation process at any time Open fixed gas valve periodically to be discharged, to improve heat transfer efficiency.
For feed liquid physical property and evaporation purpose, require, evaporator selects natural-circulation evaporator, and natural-circulation evaporator exists In evaporation process, feed liquid heats up into oven heats, and due to the saturation temperature being not up under the state, solution does not seethe with excitement. With heating and the reduction of intraductal pressure, after the temperature of solution reaches the saturation pressure under the state, come to life, so as to produce Raw a large amount of bubbles, the density of solution also reduces therewith, the not boiling of the liquid-vapor mixture so in boiling tube and circulation tube side Feed liquid between the density contrast that exists, form the circulation motive force of external-heat natural-circulation evaporator.In order to prevent fouling and crystalline substance Analysis, heating tube should be operated under the state that is totally submerged.It is not serious and the smaller solution of corrosivity that this evaporator is applied to fouling It is concentrated by evaporation, its advantage is simple in construction, is easy to manufacture, power consumption is low.The energy consumption produced during this is:System processing Amount:20m3/h;System evaporation capacity:19.8t/h;Steam consumption:26.1t/h;Installed power:16.5kw.

Claims (8)

1. a kind of gas making is containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that comprise the following steps:
(1) circulating water for gasification is after advection oil separation tank scrapes slag oil removing, by adding demulsifier by the de- steady, coalescence of oil emulsion, then Dosing coagulant, magnetic, flocculant, accelerate fat liquor, colloid and the suspended solid sediment separated out, it is heavy that the sediment is delivered to Shallow lake pond, the oil pollutant in water is removed, and the magnetic of sedimentation basin bottom is recycled by separating and recovering realization;
(2) the water outlet gravity flow on sedimentation basin top, which enters, is divided into coagulation, flocculation, air supporting three phases in flotation tank, flotation tank, past mixed Dosing coagulant makes fat liquor, colloid and suspended solid de- steady in solidifying pond, produces the sewage after small alumen ustum, coagulation and flows into flocculation Added in pond, pond flocculant by alumen ustum be collected as it is larger, be more uniformly distributed and firm alumen ustum, flocculation water and be full of microbubble Enter flotation tank after recirculated water mixing, alumen ustum flocks together with microbubble, forms uniform greasy filth cake in air supporting pool surface, so Greasy filth cake is scraped into a collecting tank afterwards;Water after treatment is flowed into absorbing well, absorption well, and the part water in absorbing well, absorption well will be in pump In the presence of, flotation tank entrance is recycled to by dissolving;
(3) after the circulation of step (2), the water outlet in flotation tank is discharged through outlet conduit, into vapo(u)rization system;Flotation tank bottom Bed mud feeding sludge-tank, i.e. complete circulating water for gasification pretreatment process;
Described vapo(u)rization system is that by the water outlet in flotation tank, i.e., pretreated circulating water for gasification is warming up to after 60 DEG C with 20 ㎡/h flow is pumped to reboiler tube side by feeding and is evaporated concentration, at the same by boiler Lai saturation life steam enter boil again The heating chamber shell side of device carries out heat exchange condensation, and condensed condensed water is returned again in boiler room through heat-exchanger pump and re-used;Gas making Recirculated water is re-fed into flash chamber after evaporation and concentration, produces substantial amounts of two secondary steam after pressure control, temperature control in flash chamber, Two secondary steam are after overheat, voltage stabilizing through being reprocessed at the top of flash chamber in feeding Gas-making Furnace;The pressure of raw steam is controlled 0.618MPa, raw vapor (steam) temperature control is 160 DEG C;Circulating water for gasification is re-fed into the evaporation capacity control in flash chamber after evaporation and concentration It is made as 19800kg/h;Two secondary steam pressure controls are 0.199MPa, and two secondary vapor (steam) temperature controls are 120 DEG C;In flash chamber Liquidus temperature control is 125 DEG C, wherein, the effective temperature difference control of liquid phase and gas phase is 34 DEG C;Flash chamber overhead vapor pressure control 0.199MPa is made as, the indirect steam amount control of flash distillation indoor top to Gas-making Furnace is 17680m3/h。
2. gas making according to claim 1 is containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that described It is that air is injected into dissolving through air compression plant after the process of step (2) is completed to be full of the recirculated water of microbubble, Dissolved in recirculated water, then the water containing saturated air delivers to the entrance release of pressure of flotation tank, release of pressure dress by pressure relief device Put the bubble of 50 to 80 microns of generation, you can obtain being full of the recirculated water of microbubble, the recirculated water for being full of microbubble easily adheres to On alumen ustum.
3. gas making according to claim 1 is containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that described Demulsifier is the 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 circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that described Coagulant is polymer alumina, and its addition is 50-120ppm.
5. gas making according to claim 1 is containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that described Flocculant is the one or more in polyacrylamide, bodied ferric sulfate or aluminium polychloride, wherein, the addition in step (1) Measure as 1-3ppm;Addition in step (2) is 0.5-1ppm.
6. gas making according to claim 1 is containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that coagulating basin Residence time be 3min;The residence time in the pond of flocculation basin is 10min;The water circulation ratio of flotation tank is 40%.
7. gas making according to claim 1 is containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that pretreatment Device includes loading coagulation degreasing unit, air-floating apparatus and vaporising device, wherein, loading coagulation degreasing unit includes mixing pit, The dosing pond of demulsifier, flocculation basin, sedimentation basin;Sedimentation basin top is connected through conveying pipeline with air supporting pool device, sedimentation basin bottom warp Pipeline is connected with magnetic recycling can again after being connected with pump, magnetic recycling can again with sludge dehydration device;Air supporting pool device includes mixed Solidifying pond and flocculation basin, bottom connection of the flocculation basin bottom through the conveying pipeline in the middle of conveying pipeline and flotation tank, flotation tank upper end is set There is outlet conduit, flotation tank bottom and bottom are additionally provided with to the pipeline of sludge-tank.
8. gas making according to claim 1 is containing ammonia containing circulation water pretreatment process of the cyanogen containing phenol, it is characterised in that described Vaporising device includes reboiler, flash chamber, and saturation life steam is connected through conveying pipeline with reboiler top, and is communicated to heating chamber shell Journey is connected;Pretreated circulating water for gasification passes to reboiler tube side through conveying pipeline is in parallel with the bottom connection of reboiler;Boil again It is connected at the top of device through conveying pipeline with flash chamber, Gas-making Furnace is connected to through conveying pipeline at the top of flash chamber;Flash chamber bottom and reboiler Bottom is connected to feed reservoir after converging through conveying pipeline;Reboiler bottom is connected to boiler room through conveying pipeline.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2696711C1 (en) * 2018-06-18 2019-08-05 Борис Семенович Ксенофонтов Method of waste water treatment

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105776476A (en) * 2016-04-25 2016-07-20 广饶康达环保水务有限公司 Magnetic-coagulation water treatment device and treatment process
CN108793555A (en) * 2018-06-13 2018-11-13 苏州永峰联环保科技有限公司 Remained ammonia treatment process and its processing system
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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1124232A (en) * 1994-12-06 1996-06-12 王师祥 Non-pollution treating tech. process for waste water in gas production
CN101781038A (en) * 2010-03-02 2010-07-21 济南冶金化工设备有限公司 Phenol and cyanogen waste water physical chemical method control process and equipment
CN102774971A (en) * 2011-05-09 2012-11-14 江苏晋煤恒盛化工有限公司 Recycling system integration apparatus used for zero discharge of sewage produced in gas making
CN203715437U (en) * 2013-12-31 2014-07-16 濮阳龙宇化工有限责任公司 Gasified low-grade heat energy recycling device
CN104310710A (en) * 2014-10-27 2015-01-28 山东省环境保护科学研究设计院 High-efficiency energy-saving treatment process for coal chemical industry wastewater
CN104386846A (en) * 2014-09-02 2015-03-04 北京熙珍坊投资管理有限公司 Treatment method and treatment system for oily sewage
WO2015131111A1 (en) * 2014-02-27 2015-09-03 Originoil, Inc. Electro-catalytic process for coalescing and skimming pollutants in bodies of water prior to filtration

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1124232A (en) * 1994-12-06 1996-06-12 王师祥 Non-pollution treating tech. process for waste water in gas production
CN101781038A (en) * 2010-03-02 2010-07-21 济南冶金化工设备有限公司 Phenol and cyanogen waste water physical chemical method control process and equipment
CN102774971A (en) * 2011-05-09 2012-11-14 江苏晋煤恒盛化工有限公司 Recycling system integration apparatus used for zero discharge of sewage produced in gas making
CN203715437U (en) * 2013-12-31 2014-07-16 濮阳龙宇化工有限责任公司 Gasified low-grade heat energy recycling device
WO2015131111A1 (en) * 2014-02-27 2015-09-03 Originoil, Inc. Electro-catalytic process for coalescing and skimming pollutants in bodies of water prior to filtration
CN104386846A (en) * 2014-09-02 2015-03-04 北京熙珍坊投资管理有限公司 Treatment method and treatment system for oily sewage
CN104310710A (en) * 2014-10-27 2015-01-28 山东省环境保护科学研究设计院 High-efficiency energy-saving treatment process for coal chemical industry wastewater

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2696711C1 (en) * 2018-06-18 2019-08-05 Борис Семенович Ксенофонтов Method of waste water treatment

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