CN107055897A - The device and processing method of a kind of combined treatment high salt and high COD sewage - Google Patents
The device and processing method of a kind of combined treatment high salt and high COD sewage Download PDFInfo
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- CN107055897A CN107055897A CN201611074833.8A CN201611074833A CN107055897A CN 107055897 A CN107055897 A CN 107055897A CN 201611074833 A CN201611074833 A CN 201611074833A CN 107055897 A CN107055897 A CN 107055897A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/06—Pressure conditions
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present invention relates to a kind of combined treatment high salt and the processing unit and processing method of high COD sewage, the sewage of the present invention passes through pretreatment stage, pretreated sewage is after regulation pH value is alkaline environment, it is directly entered oxidation evaporation reactor, make oxidation operation in sewage into carbon dioxide and water, during evaporation sewage, salt concentration in sewage, crystallization is separated out, and be calcined with semisolid into follow-up sludge roasting device, baked very small amount of inorganic salts ash content can be handled as common solid waste, also secondary recovery utilization can be carried out by purification technique again.The present invention carries out advanced oxidation, evaporation and concentration, sludge roasting process, oxidation operation in sewage is reduced into COD indexs, it is semi-solid sludge that salt concentration, crystallization in sewage, which is separated out, the sludge for evaporating the semi-solid separated out is passed through into harmless treatment after roasting, while being really achieved processing sewage, by the state of the sludge separated out in sewage together harmless treatment.
Description
Technical field
The present invention relates to a kind of physical adsorption techniques+high-level oxidation technology+(salt content exists evaporation technique combined treatment high salt
1%-20%) and high COD sewage (COD indexs are in 10000mg/L between 200000mg/L) processing unit and processing method,
Belong to technical field of sewage.
Background technology
With developing rapidly for industry, the type and quantity of sewage rapidly increase, to the pollution of water body also increasingly extensively and
Seriously, the health and safety of the mankind is threatened.The difficulty of the sewage disposal of generation also more and more higher, wherein, many high salts, high COD
Sewage processing up to standard can not be carried out with methods such as single chemical method, biochemical process, Physicals.Under the premise of such, this hair
It is bright to propose a kind of physical adsorption techniques+high-level oxidation technology+evaporation technique+roasting technology combined treatment high salt, high COD sewage
Device and handling process, effectively solve, single treatment mode can not qualified discharge the problem of, while also solving：
1. physical adsorption techniques are easily saturated, it is difficult to the problem of regenerating；
2. the problem of high-level oxidation technology quickly can not handle COD；
3. the problem of hazardous waste sludge can not be handled after evaporation.
The content of the invention
The purpose of the present invention provides a kind of combined treatment high salt, height to overcome the above mentioned problem that prior art is present
The processing unit and processing method of COD sewage.
Pretreatment stage of the present invention uses the modified active carbon adsorbent that Taiwan Guan Yu water resources scientific ＆ technical corporation is produced
(MAC), the pollutant in sewage is fast and effectively adsorbed using the ability of MAC quick adsorptions, pollutant absorption is existed
MAC table face；The ozone generator (EO3) produced simultaneously by Taiwan Guan Yu water resources scientific ＆ technical corporation, produces ozone to modification
Activated carbon adsorbent (MAC) is aerated.Make most of volatilizable organic matter (VOC) in sewage, inhaled by modified activated carbon
Removed under the ozone collective effect that attached dose (MAC) and ozone generator (EO3) are produced.
Pretreated sewage is directly entered oxidation evaporation reactor, in high temperature, height after regulation pH value is alkaline environment
Pressure is with the collective effect of oxygen, making the oxidation operation in sewage into carbon dioxide and water, while using produced by oxidation
Chemical thermal evaporation sewage, the condensation sewage after evaporation removes contained salinity substantially, and COD indexs can be reduced to biochemical standard,
Follow-up biochemical processing process can be entered.
Evaporate during sewage, salt concentration, crystallization in sewage are separated out, and are filled with semisolid into follow-up sludge roasting
Put and be calcined, baked very small amount of inorganic salts ash content can be handled as common solid waste, also can be by again
Purification technique carries out secondary recovery utilization.
The processes such as advanced oxidation, evaporation and concentration, sludge roasting can be carried out in running of the present invention simultaneously, by sewage
Oxidation operation reduces COD indexs, and it is semi-solid sludge that salt concentration, the crystallization in sewage, which are separated out, will evaporate what is separated out
The sludge of semi-solid is by harmless treatment after roasting, while being really achieved processing sewage, by the dirt separated out in sewage
The state of mud together harmless treatment.
The technical scheme is that：
A kind of processing unit of combined treatment high salt and high COD sewage, including：MAC packed towers, ozone generator EO3, in advance
Hot device A, preheater B, PH regulation reactive tank, oxidation evaporation reactor, demister, overhead gas condenser, gas-liquid separator, from
Heart liquid storage tank, cooler crystallizer, centrifugal separator, roaster, burner, pipeline and pump, it is characterised in that：Cesspool passes through pipe
Road and pump are connected with MAC packed tower upper inlets；Ozone generator EO3 ozone outlets pass through under pipeline and pump and MAC packed towers
Portion's aeration opening connection；MAC packed towers bottom outlet of sewer adjusts reactive tank wastewater inlet with PH by pipeline and is connected；PH regulations are anti-
Groove is answered to be provided with PH regulating agent imports；PH regulation reactive tank outlets of sewer are connected by pipeline and pump with preheater A low temperature imports,
Then it is connected with preheater B low temperature imports；All of above equipment constitutes preprocessing part.
Oxidation evaporation reactor top wastewater inlet is connected by pipeline with preheater B low-temperature outlets；Oxidation evaporation reaction
Device bottom oxygen inlet is connected by pipeline with oxygen tank；Oxidation evaporation reactor head steam (vapor) outlet passes through pipeline and demister
And overhead gas condenser high temperature import connection；Oxidation evaporation reactor bottom concentrated solution outlet is depressured by Liquid level adjusting valve to be dodged
It is connected after steaming with overhead gas condenser low temperature import；Overhead gas condenser hot outlet passes through pipeline and preheater B high temperature
Import is connected；Overhead gas condenser low-temperature outlet is connected by pipeline with preheater A high temperature imports；Preheater A, preheater B
Hot outlet is attached with condensation gas-liquid separator by pipeline；Overhead gas condenser bottom liquid outlet by pipeline with
Condensing crystallizer import is connected；Condensation gas-liquid separator bottom condensate outlet is connected by pipeline with subsequent treatment process
Connect；The outlet of condensation gas-liquid separator top gas is attached with outer row's interface；All of above equipment composition oxidation evaporation process
Part；
The concentrate import of cooler crystallizer top is connected by pipeline with overhead gas condenser bottom liquid outlet；Cooling
Crystalliser feet concentrated solution outlet is connected by pipeline with centrifugal separator entrance；Centrifugal separator sludge outlet is directly and sludge
Groove is connected；The fluid storage of centrifugal separator outlet of sewer is adjusted in centrifugation liquid storage tank, centrifugation liquid storage tank by pipeline and pump with PH
Save reactive tank connection；Sludge sump is attached by belt conveyor with roaster, and natural gas passes through burner with combustion air
Sludge is calcined into roaster；All of above equipment constitutes sludge roasting process part.
Described oxidation evaporation reactor is band press operation, and pressure is between 0.1MPa -0.3MPa.
The adsorbent of the filler of described MAC packed towers is the modified active carbon adsorption that Guan Yu water resources scientific ＆ technical corporation produces
Agent MAC.
Described ozone generator EO3 is the product that Guan Yu water resources scientific ＆ technical corporation produces.
The processing method of a kind of combined treatment high salt and high COD sewage ,+ozone oxidation pretreatment, oxidation are adsorbed using MAC
Evaporation process, sludge roasting processing carries out segmentation classification continuous processing to high salt and high COD sewage, it is characterised in that by following step
It is rapid to carry out：
Step 1：High salt and high COD sewage enter MAC packed towers top by cesspool by pump and pipeline, with passing through
What MAC packed towers bottom aeration plate entered, the ozone produced by ozone generator carries out fully contacting between MAC fillers, mixes,
Reaction, by most of volatilizable organic matter (VOC) in sewage, passes through modified active carbon adsorbent (MAC) and ozone generator
(EO3) removed under ozone (O3) collective effect produced；
Step 2：Pretreated sewage is carried out by pipeline into PH regulation reactive tanks by MAC packed towers, passes through peace
PH conditioning agent of the agitator by sewage with being added adjusted mounted in PH in reactive tank is sufficiently mixed, and makes the pH value of sewage
In PH:8-11 states；Then preheated by pipeline with being pumped into preheater A or preheater B；Preheater A or pre-
Hot device B thermal source comes from the gas heat in overhead gas condenser；
Step 3：Sewage after the completion of preheating enters oxidation evaporation reactor top by pipeline, by aoxidizing evaporation reaction
Device external heating device continue to be heated to after design temperature again and with the oxygen that is entered by oxidation evaporation reactor lower part high temperature,
The state of high pressure is aoxidized, evaporates reaction.A large amount of organic matters being oxidized in sewage pass through high temperature, high pressure, hyperoxia
State Quick Oxidation, and a large amount of inorganic salinities contained in sewage are evaporated concentration, sewage is changed into steam and salt
Separated, reach the COD indexs and salt index of reduction sewage；
Step 4：After the concentrate of oxidation evaporation reactor bottom is by the Liquid level adjusting valve vacuum flashing in pipe-line system
Into overhead gas condenser low temperature side；The steam that oxidation evaporation reactor head is produced enters overhead gas condenser high temperature side
Exchanged heat, cooled down with the concentrate of low temperature side；Steam after cooling enters back into preheater A, preheater B high temperature side, and low
Warm side sewage is further exchanged heat, condensation, sewage is carried out the pre-heat treatment；The mixture of condensed steam and water again
Into condensation gas-liquid separator progress gas-liquid separation, the condensed water after separation, into subsequent treatment process (for example：At bioanalysis
Science and engineering skill etc.)；Innocuous gas after separation carries out emptying process by pipeline.
Step 5：The concentrate of overhead gas condenser bottom is further crystallized into condensing crystallizer, separated out；Cooling knot
Brilliant device, which is carried in stirring at low speed device, chuck, recirculated cooling water, and the salinity in concentrate is constantly crystallized into precipitation；After precipitation
Crystallization enters centrifugal separator together with concentrate and carries out separation of solid and liquid；Fluid storage after separation is centrifuging liquid storage tank, then
Returned to by pump and pipeline in PH regulation reactive tanks and carry out circular treatment；Solid after separation enters in sludge sump；
Step 6：Sludge in sludge sump is sent into roaster by belt conveyor and roasted after accumulation is a certain amount of
Burn；Burner is calcined using natural gas as fuel, by more than 900 DEG C of burning of sludge progress, directly by having in sludge
Machine burning is removed, and remaining inorganic salts can be handled as Conventional solid discarded object；As having recovery value in inorganic salts
Inorganic salts, also inorganic salts can further be purified by subsequently adding purifying plant, reclaim.
MAC filler in packed column uses the modified active carbon adsorption that Taiwan Guan Yu water resources scientific ＆ technical corporation is produced in the present invention
Agent (MAC), is fast and effectively adsorbed to the pollutant in sewage using the ability of MAC quick adsorptions, pollutant is adsorbed
In MAC table face；Then, the ozone gas that the ozone generator (EO3) produced by Taiwan Guan Yu water resources scientific ＆ technical corporation is produced
Body, to MAC, makes ozone be adsorbed by MAC table face and be catalyzed generation hydroxyl radical free radical (OH)；OH free radicals are again to MAC table face
Pollutant carry out depth oxidation processes, VOC pollutants is rapidly and thoroughly degraded to the material of environmental sound.Together
When, the pollutant for being adsorbed in MAC table face is disposed of, and MAC is in undersaturated condition all the time, reduces the demand of regeneration.This
Backwash need not be carried out to MAC, ozone can be combined during operation, fast and effectively the pollutant in water is carried out in invention running
Oxidation, strong adaptability, processing speed is fast, and floor space is greatly reduced.
Brief description of the drawings
Fig. 1 is decomposed into the degraded of hydroxyl radical free radical (OH) and COD organic matters for the ozone (O3) in the MAC table face of the present invention
Schematic diagram.
Fig. 2 is schematic flow sheet of the invention.
Fig. 3 is apparatus structure schematic diagram of the invention.
In figure：R-A is ozone generator EO3, and S-A is MAC packed towers, and E-A is preheater A, and E-B is preheater B, T-01
For oxygen tank, T-02 is that PH adjusts reactive tank, and T-04 is centrifugation liquid storage tank, and S-02 is centrifugal separator, and R-02 is roaster, C-
03 is condensation gas-liquid separator, and R-01 is burner, and C-01 is oxidation evaporation reactor, and S-03 is demister, and C-02 is tower top
Gas condenser, S-01 is cooler crystallizer, and P-01, P-02, P-03 are pump.
Embodiment
As shown in figure 3, the inventive system comprises：Ozone generator EO3 (R-A), MAC packed towers (S-A), preheater A
(E-A), preheater B (E-B), PH regulation reactive tank (T-02), centrifugation liquid storage tank (T-04), centrifugal separator (S-02), roasting
Stove (R-02), condensation gas-liquid separator (C-03), burner (R-01), oxidation evaporation reactor (C-01), demister (S-03),
Overhead gas condenser (C-02), cooler crystallizer (S-01), pump, pipeline etc., it is characterised in that：Cesspool by a pipeline and
Pump is connected with MAC packed tower upper inlets；Ozone generator EO3 ozone outlets pass through a pipeline and pump and MAC packed towers bottom
Aeration opening is connected；MAC packed towers bottom outlet of sewer adjusts reactive tank wastewater inlet with PH by a pipeline and is connected；PH regulations are anti-
Groove is answered to be provided with PH regulating agent imports；PH regulation reactive tank outlets of sewer are connected by pipeline and pump with preheater A low temperature imports,
Then it is connected with preheater B low temperature imports；All of above equipment constitutes preprocessing part.
Oxidation evaporation reactor top wastewater inlet is connected by pipeline with preheater B low-temperature outlets；Oxidation evaporation reaction
Device bottom oxygen inlet is connected by pipeline with oxygen tank；Oxidation evaporation reactor head steam (vapor) outlet passes through pipeline and demister
And overhead gas condenser high temperature import connection；Oxidation evaporation reactor bottom concentrated solution outlet is depressured by Liquid level adjusting valve to be dodged
It is connected after steaming with overhead gas condenser low temperature import；Overhead gas condenser hot outlet passes through pipeline and preheater B high temperature
Import is connected；Overhead gas condenser low-temperature outlet is connected by pipeline with preheater A high temperature imports；Preheater A, preheater B
Hot outlet is attached with condensation gas-liquid separator by pipeline；Overhead gas condenser bottom liquid outlet by pipeline with
Condensing crystallizer import is connected；Condensation gas-liquid separator bottom condensate outlet is connected by pipeline with subsequent treatment process
Connect；The outlet of condensation gas-liquid separator top gas is attached with outer row's interface；All of above equipment composition oxidation evaporation process
Part；
The concentrate import of cooler crystallizer top is connected by pipeline with overhead gas condenser bottom liquid outlet；Cooling
Crystalliser feet concentrated solution outlet is connected by pipeline with centrifugal separator entrance；Centrifugal separator sludge outlet is directly and sludge
Groove is connected；The fluid storage of centrifugal separator outlet of sewer is adjusted in centrifugation liquid storage tank, centrifugation liquid storage tank by pipeline and pump with PH
Save reactive tank connection；Sludge sump is attached by belt conveyor with roaster；Natural gas passes through burner with combustion air
Sludge is calcined into roaster, all of above equipment constitutes sludge roasting process part.
Described oxidation evaporation reactor is band press operation, and pressure is between 0.1MPa -0.3MPa.
The adsorbent of the filler of described MAC packed towers is the modified active carbon adsorption that Guan Yu water resources scientific ＆ technical corporation produces
Agent MAC.
Described ozone generator EO3 is the product that Guan Yu water resources scientific ＆ technical corporation produces.
The processing method of a kind of combined treatment high salt and high COD sewage ,+ozone oxidation pretreatment, oxidation are adsorbed using MAC
Evaporation treatment process, sludge roasting handling process carries out segmentation classification continuous processing to high salt, high COD sewage, as shown in Fig. 2
It is characterized in that carrying out according to the following steps：
Step 1：High salt and high COD sewage enter MAC packed towers top by cesspool by pump and pipeline, with passing through
What MAC packed towers bottom aeration plate entered, the ozone produced by ozone generator carries out fully contacting between MAC fillers, mixes,
Reaction, by most of volatilizable organic matter (VOC) in sewage, passes through modified active carbon adsorbent (MAC) and ozone generator
(EO3) removed under ozone (O3) collective effect produced；
Step 2：Pretreated sewage is carried out by pipeline into PH regulation reactive tanks by MAC packed towers, passes through peace
PH conditioning agent of the agitator by sewage with being added adjusted mounted in PH in reactive tank is sufficiently mixed, and makes the pH value of sewage
In PH:8-11 states；Then preheated by pipeline with being pumped into preheater A or preheater B；Preheater A or pre-
Hot device B thermal source comes from the gas heat in overhead gas condenser；
Step 3：Sewage after the completion of preheating enters oxidation evaporation reactor top by pipeline, by aoxidizing evaporation reaction
Device external heating device continue to be heated to after design temperature again and with the oxygen that is entered by oxidation evaporation reactor lower part high temperature,
The state of high pressure is aoxidized, evaporates reaction.A large amount of organic matters being oxidized in sewage pass through high temperature, high pressure, hyperoxia
State Quick Oxidation, and a large amount of inorganic salinities contained in sewage are evaporated concentration, sewage is changed into steam and salt
Separated, reach the COD indexs and salt index of reduction sewage；
Step 4：After the concentrate of oxidation evaporation reactor bottom is by the Liquid level adjusting valve vacuum flashing in pipe-line system
Into overhead gas condenser low temperature side；The steam that oxidation evaporation reactor head is produced enters overhead gas condenser high temperature side
Exchanged heat, cooled down with the concentrate of low temperature side；Steam after cooling enters back into preheater A, preheater B high temperature side, and low
Warm side sewage is further exchanged heat, condensation, sewage is carried out the pre-heat treatment；The mixture of condensed steam and water again
Into condensation gas-liquid separator progress gas-liquid separation, the condensed water after separation, into subsequent treatment process (for example：At bioanalysis
Science and engineering skill etc.)；Innocuous gas after separation carries out emptying process by pipeline.
Step 5：The concentrate of overhead gas condenser bottom is further crystallized into condensing crystallizer, separated out；Cooling knot
Brilliant device, which is carried in stirring at low speed device, chuck, recirculated cooling water, and the salinity in concentrate is constantly crystallized into precipitation；After precipitation
Crystallization enters centrifugal separator together with concentrate and carries out separation of solid and liquid；Fluid storage after separation is centrifuging liquid storage tank, then
Returned to by pump and pipeline in PH regulation reactive tanks and carry out circular treatment；Solid after separation enters in sludge sump；
Step 6：Sludge in sludge sump is sent into roaster by belt conveyor and roasted after accumulation is a certain amount of
Burn；Burner is calcined using natural gas as fuel, by more than 900 DEG C of burning of sludge progress, directly by having in sludge
Machine burning is removed, and remaining inorganic salts can be handled as Conventional solid discarded object；As having recovery value in inorganic salts
Inorganic salts, also inorganic salts can further be purified by subsequently adding purifying plant, reclaim.
The operation principle and feature of the present invention：
Traditional processing mode separates oxidation processes with evaporation process, for example multiple-effect evaporation technology and MVR on the market
Technology etc. is all traditional evaporation technology, and this technique only has desalination, condensing crystallizing effect, but to contained substantial amounts of in sewage
Organic matter can not directly be removed and stayed in strong brine, the sludge that evaporation technique is produced is turned into dangerous waste；For another example on the market
Wet air oxidation technology (WAO) oxidation processes can only be carried out to the organic matter in sewage, but can not to the salt contained by it
Remove.Two kinds of foregoing technologies can not all face high salt, the sewage of high COD indexs.
The present invention coordinates follow-up oxidation evaporation technique, while sharp using the preconditioning technique of physical absorption+advanced oxidation
Sludge roasting technology is used, while sewage is purified, can accomplish that sewage sludge harmlessness is handled.
The preconditioning technique of physical absorption+advanced oxidation is the MAC absorption produced using Guan Yu water resources scientific ＆ technical corporation
Agent.MAC adsorbents are different from traditional activated carbon adsorbent.It is by the dirt in sewage in traditional activated carbon adsorbent adsorption process
Dye thing is adsorbed enter in the hole of activated carbon surface, is difficult to go by simple backwash mode enter in activated carbon hole once adsorbing
Remove, COD pollutants are difficult to pass in and out pore, so the adsorption capacity of conventional adsorbent is low, service life is not high.And the present invention is used
Guan Yu water resources scientific ＆ technical corporation modified active carbon adsorbent MAC, using the physical action of surface functional group, draw through electrostatic
Power or the Fan Dewa power of hearing, the pollutant in sewage is adsorbed in MAC adsorbent surfaces, then is produced by MAC sorbent catalysts ozone
Raw hydroxyl radical free radical (OH), carries out advanced oxidation processing (AOP), directly oxidizes away the COD pollutants of adsorbent surface.
As shown in figure 1, so MAC adsorbents are just renewable, repeat absorption.The starting material source for making MAC adsorbents is a lot, bag
Include：Activated carbon (comes from coconut husk, pitch, or ature of coal), and exploitation is MAC adsorbents by starting material of agricultural waste.The present invention
One of inventor, the research of twice laid has been applied to become into Chinese patent, and " CN103787443A- is solid to remove total solution property
Body flows through formula absorber ".
Oxidation evaporation technique of the present invention is can be by organic matter Quick Oxidation under high temperature, high pressure using oxygen
Into carbon dioxide and water, while being evaporated using the chemical heat produced by oxidation to the moisture content in sewage, the salt in sewage
The principle of progress condensing crystallizing is carried out sewage and handled.Existing oxidation reaction in its processing procedure, while also there is evaporation process, makes
It has extraordinary effect in for high salt, high COD sewage disposal.
The present invention uses sludge roasting technology, can be fast and effectively decomposed at high operating temperatures using organic matter
Principle, sludge is rapidly heated in roasting process to more than 900 DEG C, the organic matter in sludge is quickly decomposed, remain
Under inorganic salts can be handled as solid waste, also can recycling by purifying technique again.
The present apparatus can according to contained by sewage salt, the different demands of COD indexs, data are entered by on-line computing model
Row online acquisition, and by PLC processing, the indexs such as reaction time are evaporated in the inflow of regulating system, amount of oxygen, oxidation.
Adapt to a variety of different high salts, high COD sewage.
Claims (10)
1. the processing unit of a kind of combined treatment high salt and high COD sewage, including：MAC packed towers, ozone generator EO3, preheating
Device A, preheater B, PH regulation reactive tank, oxidation evaporation reactor, demister, overhead gas condenser, gas-liquid separator, centrifugation
Liquid storage tank, cooler crystallizer, centrifugal separator, roaster, burner, pipeline and pump, it is characterised in that：Cesspool passes through pipeline
It is connected with pump with MAC packed tower upper inlets；Ozone generator EO3 ozone outlets pass through pipeline and pump and MAC packed towers bottom
Aeration opening is connected；MAC packed towers bottom outlet of sewer adjusts reactive tank wastewater inlet with PH by pipeline and is connected；PH regulation reactions
Groove is provided with PH regulating agent imports；PH regulation reactive tank outlets of sewer are connected by pipeline and pump with preheater A low temperature imports, with
It is connected afterwards with preheater B low temperature imports；All of above equipment constitutes preprocessing part；
Oxidation evaporation reactor top wastewater inlet is connected by pipeline with preheater B low-temperature outlets；Under oxidation evaporation reactor
Portion's oxygen inlet is connected by pipeline with oxygen tank；Oxidation evaporation reactor head steam (vapor) outlet passes through pipeline and demister and tower
The import of top gas condenser body high temperature is connected；After oxidation evaporation reactor bottom concentrated solution outlet is by Liquid level adjusting valve decompression flash distillation
It is connected with overhead gas condenser low temperature import；Overhead gas condenser hot outlet passes through pipeline and preheater B high temperature imports
Connection；Overhead gas condenser low-temperature outlet is connected by pipeline with preheater A high temperature imports；Preheater A, preheater B high temperature
Outlet is attached with condensation gas-liquid separator by pipeline；Overhead gas condenser bottom liquid outlet passes through pipeline and condensation
Crystallizer import is connected；Condensation gas-liquid separator bottom condensate outlet is attached by pipeline with subsequent treatment process；It is cold
Solidifying gas-liquid separator top gas outlet is attached with outer row's interface；All of above equipment composition oxidation evaporation process part；
The concentrate import of cooler crystallizer top is connected by pipeline with overhead gas condenser bottom liquid outlet；Crystallisation by cooling
Device bottom concentrated solution outlet is connected by pipeline with centrifugal separator entrance；Centrifugal separator sludge outlet directly connects with sludge sump
Connect；The fluid storage of centrifugal separator outlet of sewer adjusts anti-by pipeline and pump in centrifugation liquid storage tank, centrifugation liquid storage tank with PH
Groove is answered to connect；Sludge sump is attached by belt conveyor with roaster, and natural gas is entered with combustion air by burner
Sludge is calcined in roaster；All of above equipment constitutes sludge roasting process part.
2. the device of combined treatment high salt according to claim 1 and high COD sewage, it is characterised in that：Described oxidation
It is band press operation to evaporate reactor, and pressure is between 0.1MPa -0.3MPa.
3. the device of combined treatment high salt according to claim 1 and high COD sewage, it is characterised in that：The MAC fillers
The adsorbent of the filler of tower is the modified active carbon adsorbent MAC that Guan Yu water resources scientific ＆ technical corporation produces.
4. the device of combined treatment high salt according to claim 1 and high COD sewage, it is characterised in that：Described ozone
Generator EO3 is the product that Guan Yu water resources scientific ＆ technical corporation produces.
5. using combined treatment high salt and the processing method of the device of high COD sewage described in one of claim 1-4, use
MAC absorption+ozone oxidation pretreatment, aoxidizes evaporation process, and sludge roasting processing carries out segmentation classification to high salt and high COD sewage
Continuous processing, it is characterised in that carry out according to the following steps：
Step 1：High salt and high COD sewage enter MAC packed towers top by cesspool by pump and pipeline, with being filled out by MAC
Expect what tower bottom aeration plate entered, the ozone produced by ozone generator carries out fully contacting between MAC fillers, mixes, reacts,
By most of volatilizable organic matter (VOC) in sewage, pass through modified active carbon adsorbent (MAC) and ozone generator (EO3)
Removed under ozone (O3) collective effect of generation；
Step 2：Pretreated sewage is carried out by MAC packed towers PH is entered by pipeline to adjust reactive tank, by installed in
PH conditioning agent of the agitator by sewage with being added that PH is adjusted in reactive tank is sufficiently mixed, and is in the pH value of sewage
PH:8-11 states；Then preheated by pipeline with being pumped into preheater A and preheater B；Preheater A and preheater B
Thermal source come from the gas heat of overhead gas condenser；
Step 3：Sewage after the completion of preheating enters oxidation evaporation reactor top by pipeline, by aoxidizing outside evaporation reactor
Portion's heater continues to be heated to after design temperature again and with the oxygen by oxidation evaporation reactor lower part entrance in high temperature, high pressure
State aoxidized, evaporate reaction.A large amount of organic matters being oxidized in sewage pass through high temperature, high pressure, the state of hyperoxia
Quick Oxidation, and a large amount of inorganic salinities contained in sewage are evaporated concentration, sewage is changed into steam and enter with salinity
Row separation, reaches the COD indexs and salt index of reduction sewage；
Step 4：The concentrate of oxidation evaporation reactor bottom after the Liquid level adjusting valve vacuum flashing in pipe-line system by entering
Overhead gas condenser low temperature side；Oxidation evaporation reactor head produce steam enter overhead gas condenser high temperature side with it is low
The concentrate of warm side is exchanged heat, cooled down；Steam after cooling enters back into preheater A, preheater B high temperature side, with low temperature side
Sewage is further exchanged heat, condensation, sewage is carried out the pre-heat treatment；The mixture of condensed steam and water enters again
Condense gas-liquid separator and carry out gas-liquid separation, the condensed water after separation, into subsequent treatment process；Innocuous gas after separation leads to
Piping carries out emptying process.
Step 5：The concentrate of overhead gas condenser bottom is further crystallized into condensing crystallizer, separated out；Cooler crystallizer
With stirring at low speed device, there is recirculated cooling water in chuck, the salinity in concentrate is constantly crystallized into precipitation；Crystallization after precipitation
Enter centrifugal separator together with concentrate and carry out separation of solid and liquid；Fluid storage after separation then passes through in centrifugation liquid storage tank
Pump and pipeline return in PH regulation reactive tanks and carry out circular treatment；Solid after separation enters in sludge sump；
Step 6：Sludge in sludge sump is sent into roaster by belt conveyor and is calcined after accumulation is a certain amount of；Roasting
Burner is burnt using natural gas as fuel, by more than 900 DEG C of burning of sludge progress, directly by the organic combustion in sludge
Remove, remaining inorganic salts can be handled as Conventional solid discarded object；As having the inorganic of recovery value in inorganic salts
Salt, also can further be purified inorganic salts by subsequently adding purifying plant, be reclaimed.
6. the processing method of the device of combined treatment high salt according to claim 5 and high COD sewage, it is characterised in that：
The oxidation evaporation reactor is evaporated processing using the chemical heat produced by oxidation.
7. the processing method of the device of combined treatment high salt according to claim 5 and high COD sewage, it is characterised in that：
The oxidation evaporation reactor bottom thickened sludge is depressured by liquid level mediation valve.
8. the processing method of the device of combined treatment high salt according to claim 5 and high COD sewage, it is characterised in that：
The oxidation evaporation reactor head steam is exchanged heat by overhead gas condenser and thickened sludge, and the water allowed in sludge is again
Degree evaporation.
9. the processing method of the device of combined treatment high salt according to claim 5 and high COD sewage, it is characterised in that：
The gas that the sewage entered before oxidation evaporation reactor is come out by preheater A, preheater B and overhead gas condenser enters
Row heat exchange.
10. the processing method of the device of combined treatment high salt according to claim 5 and high COD sewage, it is characterised in that：
Steam after being cooled by preheater A, preheater B is separated with condensed water mixture by condensing gas-liquid separator.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108675531A (en) * | 2018-05-17 | 2018-10-19 | 海若斯（北京）环境科技有限公司 | The thermochemical treatment system and method for high organic waste liquid with high salt |
| CN110386706A (en) * | 2018-04-20 | 2019-10-29 | 姜林 | A kind for the treatment of high-concentration saline organic wastewater processing system and method |
| CN112110588A (en) * | 2020-09-27 | 2020-12-22 | 山东理工大学 | Treatment method and treatment system for medium-high temperature MVR wastewater of degradable organic matter |
| CN112811686A (en) * | 2020-12-07 | 2021-05-18 | 德阳一铭科技发展有限公司 | Natural gas exploitation wastewater treatment process |
| CN113683146A (en) * | 2021-08-23 | 2021-11-23 | 安徽智泓净化科技股份有限公司 | Multi-membrane integration-evaporative crystallization coupling system for water treatment |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TW200819397A (en) * | 2006-10-31 | 2008-05-01 | Zhi-Zhong Chen | Wastewater treatment method and apparatus thereof |
| CN103848530A (en) * | 2014-03-03 | 2014-06-11 | 无锡市中岳石化设备有限公司 | DDISO-integrated synchronous oxidation and desalination device |
| CN105461128A (en) * | 2015-12-18 | 2016-04-06 | 碳氢技术工程管理（武汉）有限公司 | Device and method for treating high COD (Chemical Oxygen Demand) sewage in combined way |
| CN206417959U (en) * | 2016-11-29 | 2017-08-18 | 碳氢技术工程管理（武汉）有限公司 | A kind of device of combined treatment high salt and high COD sewage |
-
2016
- 2016-11-29 CN CN201611074833.8A patent/CN107055897A/en not_active Withdrawn
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TW200819397A (en) * | 2006-10-31 | 2008-05-01 | Zhi-Zhong Chen | Wastewater treatment method and apparatus thereof |
| CN103848530A (en) * | 2014-03-03 | 2014-06-11 | 无锡市中岳石化设备有限公司 | DDISO-integrated synchronous oxidation and desalination device |
| CN105461128A (en) * | 2015-12-18 | 2016-04-06 | 碳氢技术工程管理（武汉）有限公司 | Device and method for treating high COD (Chemical Oxygen Demand) sewage in combined way |
| CN206417959U (en) * | 2016-11-29 | 2017-08-18 | 碳氢技术工程管理（武汉）有限公司 | A kind of device of combined treatment high salt and high COD sewage |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110386706A (en) * | 2018-04-20 | 2019-10-29 | 姜林 | A kind for the treatment of high-concentration saline organic wastewater processing system and method |
| CN108675531A (en) * | 2018-05-17 | 2018-10-19 | 海若斯（北京）环境科技有限公司 | The thermochemical treatment system and method for high organic waste liquid with high salt |
| CN112110588A (en) * | 2020-09-27 | 2020-12-22 | 山东理工大学 | Treatment method and treatment system for medium-high temperature MVR wastewater of degradable organic matter |
| WO2022062552A1 (en) * | 2020-09-27 | 2022-03-31 | 山东理工大学 | Medium-to-high-temperature mvr wastewater treatment method and system capable of degrading organic matter |
| CN112811686A (en) * | 2020-12-07 | 2021-05-18 | 德阳一铭科技发展有限公司 | Natural gas exploitation wastewater treatment process |
| CN113683146A (en) * | 2021-08-23 | 2021-11-23 | 安徽智泓净化科技股份有限公司 | Multi-membrane integration-evaporative crystallization coupling system for water treatment |
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