CN110078326A - Biochemical sludge processing system and method - Google Patents
Biochemical sludge processing system and method Download PDFInfo
- Publication number
- CN110078326A CN110078326A CN201910372302.4A CN201910372302A CN110078326A CN 110078326 A CN110078326 A CN 110078326A CN 201910372302 A CN201910372302 A CN 201910372302A CN 110078326 A CN110078326 A CN 110078326A
- Authority
- CN
- China
- Prior art keywords
- biochemical sludge
- tower
- deamination
- oxidation solution
- ammonia
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000010802 sludge Substances 0.000 title claims abstract description 108
- 238000012545 processing Methods 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title abstract description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 104
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 90
- 230000003647 oxidation Effects 0.000 claims abstract description 88
- 239000007788 liquid Substances 0.000 claims abstract description 69
- 230000009615 deamination Effects 0.000 claims abstract description 60
- 238000006481 deamination reaction Methods 0.000 claims abstract description 60
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 52
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 44
- 230000001590 oxidative effect Effects 0.000 claims abstract description 41
- 238000005406 washing Methods 0.000 claims abstract description 37
- 238000010438 heat treatment Methods 0.000 claims abstract description 32
- 230000003197 catalytic effect Effects 0.000 claims abstract description 26
- 238000010000 carbonizing Methods 0.000 claims abstract description 17
- 239000003002 pH adjusting agent Substances 0.000 claims abstract description 13
- 230000000694 effects Effects 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 32
- 239000000706 filtrate Substances 0.000 claims description 21
- 238000001704 evaporation Methods 0.000 claims description 20
- 230000008020 evaporation Effects 0.000 claims description 20
- 238000011084 recovery Methods 0.000 claims description 20
- 239000003814 drug Substances 0.000 claims description 17
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 16
- 230000003750 conditioning effect Effects 0.000 claims description 16
- 238000003763 carbonization Methods 0.000 claims description 14
- 238000004062 sedimentation Methods 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 9
- 239000012752 auxiliary agent Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 6
- 230000006837 decompression Effects 0.000 claims description 6
- 238000003672 processing method Methods 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims description 2
- 230000015556 catabolic process Effects 0.000 abstract description 7
- 238000006731 degradation reaction Methods 0.000 abstract description 7
- 230000009467 reduction Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 52
- 239000010865 sewage Substances 0.000 description 9
- 238000010586 diagram Methods 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 238000003303 reheating Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000005255 carburizing Methods 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 210000004027 cell Anatomy 0.000 description 2
- 210000000170 cell membrane Anatomy 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000000701 coagulant Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 239000000575 pesticide Substances 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 241000585116 Galba truncatula Species 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000001680 brushing effect Effects 0.000 description 1
- 210000002421 cell wall Anatomy 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000003760 hair shine Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000009279 wet oxidation reaction Methods 0.000 description 1
Classifications
-
- 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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention belongs to offal treatment field, disclosing a kind of biochemical sludge processing system and method, system includes sequentially connected heating device, carbonizing plant, catalytic oxidizing equipment, ammonia removal device and call-back device；Heating device, for biochemical sludge to be processed to be heated to the first preset temperature；Carbonizing plant, for making the biochemical sludge for being heated to the first preset temperature be decomposed into upper liquid and lower layer's pug under conditions of temperature-pressure；Catalytic oxidizing equipment is provided with catalysis oxidation area, for making upper liquid in catalysis oxidation area and air effect, generates oxidation solution；Ammonia removal device generates deamination tail washings for the oxidation solution after cooling down with except ammonia pharmacy effect；Call-back device generates relief liquor for acting on deamination tail washings and pH adjusting agent.Biochemical sludge is changed into the relief liquor and carbonized residue of easy biochemical degradation by biochemical sludge processing system provided by the invention, and sludge reduction, harmless treatment are thorough, and cost is relatively low for integrated treatment.
Description
Technical field
The invention belongs to offal treatment fields, are to be related to a kind of biochemical sludge processing system and method more specifically.
Background technique
Biochemical sludge refers to the excess sludge of municipal administration or the discharge of industrial park biochemical sewage treatment system.At biochemical sewage
Reason system handles a large amount of sanitary wastewater and/or industrial wastewater daily, and (referred to herein as preprocessed mistake, reaches biochemical degradation and refers to
Target industrial wastewater), thus can also generate a large amount of biochemical sludge.In existing biochemical sewage treatment system, every processing 10,000 is vertical
Square municipal wastewater can generate 5-10 tons of biochemical sludge.Existing biochemical sludge processing main path is set by sludge pressing
It is standby, the moisture of biochemical sludge is reduced, cement plant is then transported to and is further processed.
The main component of biochemical sludge includes water, microorganism " corpse ", organic pollutant, inorganic matter etc..To biochemical sludge
In the process of processing, highly concentrated brine waste (COD concentration is high) can be generated, secondary pollution is formed, processing cost is high.
Summary of the invention
The purpose of the present invention is to provide a kind of biochemical sludge processing systems, are handled with solving biochemical sludge in the prior art
Difficulty, the high problem of processing cost.
To achieve the above object, the technical solution adopted by the present invention is that: a kind of biochemical sludge processing system is provided, including according to
Heating device, carbonizing plant, catalytic oxidizing equipment, ammonia removal device and the call-back device of secondary connection；
The heating device, for biochemical sludge to be processed to be heated to the first preset temperature；
The carbonizing plant is heated to the described biochemical dirty of the first preset temperature for making under conditions of temperature-pressure
Mud is decomposed into upper liquid and lower layer's pug；
The catalytic oxidizing equipment is provided with catalysis oxidation area, for make the upper liquid the catalysis oxidation area with
Air effect generates oxidation solution, and the temperature for inputting the air in the catalysis oxidation area is the second preset temperature；
The ammonia removal device generates deamination tail washings for the oxidation solution after cooling down with except ammonia pharmacy effect, described
The ammonia nitrogen concentration of deamination tail washings is lower than the ammonia nitrogen concentration of the oxidation solution；
The call-back device, for acting on the deamination tail washings and pH adjusting agent, generation relief liquor, the relief liquor
PH value is specified pH value.
Optionally, the heating device includes sequentially connected medicament adding unit, preheating unit and hot cell again；It is described
Catalytic oxidizing equipment includes heat recovery unit；
The medicament adding unit, for thermal oxide auxiliary agent to be added in the biochemical sludge by specified proportion；
There are heat transfers between the preheating unit and the heat recovery unit；The preheating unit is used for from institute
It states heat recovery unit and absorbs heat, the heating biochemical sludge that thermal oxide auxiliary agent has been added；The heat recovery unit is used
In the heat of the oxidation solution before cooling is supplied to the preheating unit, the temperature of the oxidation solution is reduced；
The hot cell again makes the biochemistry for heating to the biochemical sludge after preheating unit heating
Sludge reaches first preset temperature.
Optionally, the carbonizing plant includes carbonization sedimentation tower, and the carbonization sedimentation tower includes tower body, feed inlet, above goes out
Material mouth, lower discharge port；
The feed inlet is set in the middle part of tower body, and the biochemical sludge flows into inside the tower body from the feed inlet；
Inside the tower body, it is provided with above the feed inlet and blocks mud inclined plate；
The top discharge mouth is set at the top of the tower body, for the upper liquid to be discharged；
The lower discharge port is set to the tower body bottom, for lower layer's pug to be discharged；
The lower discharge port is connected with pug discharging adapter tube, pug discharging solenoid valve in turn and by material container.
Optionally, the catalytic oxidizing equipment includes catalysis oxidizing tower, and the catalysis oxidizing tower is provided with gas-liquid feed inlet
With oxidation solution discharge port, the catalysis oxidation area is set to inside the tower body of the catalysis oxidizing tower, and the gas-liquid feed inlet is set
It is placed in the bottom of the catalysis oxidizing tower, the oxidation solution discharge port is set to the top of the catalysis oxidizing tower.
Optionally, the catalytic oxidizing equipment further includes gas-liquid separator, and the gas-liquid separator goes out with the oxidation solution
Material mouth connection, the gas-liquid separator are used to separate oxidation solution and by the air generations for inputting the catalysis oxidation area
Tail gas.
Optionally, the ammonia removal device includes decompressor, dosing reactor tank, filter device；
The decompressor is provided with decompression input end and relief outlet end, the decompression input end and the heat recovery
Unit connection；
The dosing reactor tank is provided with oxidation solution entrance, except ammonia medicament entrance and reaction solution export, the relief outlet
End is connect with the oxidation solution entrance；
The filter device includes filtering entrance and filtrate (liquid, and the filtering entrance and reaction solution outlet connect.
Optionally, the ammonia removal device further includes flash evaporation deamination tower, and the flash evaporation deamination tower is provided with filtrate import, cloth liquid
Pipe, the outlet of the first air inlet, the second air inlet, the first gas distribution pipe, the second gas distribution pipe, packed bed, tail washings and deamination exhaust outlet；
The filtrate import is set to the middle and upper part of the flash evaporation deamination tower tower body, external to connect with the filtrate (liquid,
Inside is connect with the liquid distributor being set to inside tower body；
First air inlet, the second air inlet are respectively arranged at the middle and lower part of the flash evaporation deamination tower tower body, and described
It is connect inside one air inlet with first gas distribution pipe being set to inside tower body, inside second air inlet and is set to tower
Second gas distribution pipe connection in internal portion；
Top in first gas distribution pipe and second gas distribution pipe, the lower section of the liquid distributor are provided with described
Packed bed；
The tail washings outlet is set to the bottom of the flash evaporation deamination tower；
The deamination exhaust outlet is set to the top of the flash evaporation deamination tower.
It optionally, further include ammonia absorption device, the ammonia absorption device is connect with the deamination exhaust outlet.
Optionally, the call-back device includes pH conditioning tank, pH tester and soda acid chemicals dosing plant；
The pH conditioning tank, for accommodating the deamination tail washings；
The pH tester, for measuring the pH value of liquid in the pH conditioning tank；
The soda acid chemicals dosing plant, for the pH adjusting agent to be added toward the pH conditioning tank.
The present invention also provides a kind of biochemical sludge processing methods, comprising:
Biochemical sludge to be processed is heated to the first preset temperature；
Under the conditions of preset temperature-pressure, the biochemical sludge for being heated to the first preset temperature is made to be decomposed into upper liquid
With lower layer's pug；
So that the upper liquid is carried out catalysed oxidn under the second preset temperature, generates oxidation solution；
By decrease temperature and pressure device to the oxidation solution decrease temperature and pressure, by the oxidation solution after decrease temperature and pressure and ammonia is removed
Medicament reaction, generates deamination tail washings, and the ammonia nitrogen concentration of the deamination tail washings is lower than the ammonia nitrogen concentration of the oxidation solution；
It reacts the deamination tail washings with pH adjusting agent, generates relief liquor, the pH value of the relief liquor is specified pH value.
The beneficial effect of biochemical sludge processing system and method provided by the invention is: compared with prior art, biochemical
Under temperature-pressure and catalytic condition, biochemical sludge is changed into easily sludge treating system by organic matter in efficient degradation sludge
The relief liquor and carbonized residue of biochemical degradation, sludge reduction, harmless treatment are thorough, and cost is relatively low for integrated treatment.
Detailed description of the invention
It to describe the technical solutions in the embodiments of the present invention more clearly, below will be to embodiment or description of the prior art
Needed in attached drawing be briefly described, it should be apparent that, the accompanying drawings in the following description is only of the invention some
Embodiment for those of ordinary skill in the art without any creative labor, can also be according to these
Attached drawing obtains other attached drawings.
Fig. 1 is the structural schematic diagram of biochemical sludge processing system provided in an embodiment of the present invention；
Fig. 2 is the structural schematic diagram of heating device provided in an embodiment of the present invention；
Fig. 3 is the structural schematic diagram of carbonization sedimentation tower provided in an embodiment of the present invention；
Fig. 4 is the structural schematic diagram of catalysis oxidizing tower provided in an embodiment of the present invention；
Fig. 5 is the structural schematic diagram of flash evaporation deamination tower provided in an embodiment of the present invention；
Fig. 6 is the flow diagram of biochemical sludge processing method provided in an embodiment of the present invention.
Specific embodiment
In order to which technical problems, technical solutions and advantages to be solved are more clearly understood, tie below
Accompanying drawings and embodiments are closed, the present invention will be described in further detail.It should be appreciated that specific embodiment described herein is only
To explain the present invention, it is not intended to limit the present invention.
It should be noted that it can be directly another when element is referred to as " being fixed on " or " being set to " another element
On one element or indirectly on another element.When an element is known as " being connected to " another element, it can
To be directly to another element or be indirectly connected on another element.
It is to be appreciated that term " length ", " width ", "upper", "lower", "front", "rear", "left", "right", "vertical",
The orientation or positional relationship of the instructions such as "horizontal", "top", "bottom" "inner", "outside" is that orientation based on the figure or position are closed
System, is merely for convenience of description of the present invention and simplification of the description, rather than the device or element of indication or suggestion meaning must have
Specific orientation is constructed and operated in a specific orientation, therefore is not considered as limiting the invention.
In addition, term " first ", " second " are used for descriptive purposes only and cannot be understood as indicating or suggesting relative importance
Or implicitly indicate the quantity of indicated technical characteristic.Define " first " as a result, the feature of " second " can be expressed or
Implicitly include one or more of the features.In the description of the present invention, the meaning of " plurality " is two or more,
Unless otherwise specifically defined.
As shown in Figure 1, existing be illustrated biochemical sludge processing system provided in an embodiment of the present invention.Biochemical sludge processing
System includes sequentially connected heating device 10, carbonizing plant 20, catalytic oxidizing equipment 30, ammonia removal device 40 and call-back device
50；
The heating device 10, for biochemical sludge to be processed to be heated to the first preset temperature；
The carbonizing plant 20, for making the biochemistry for being heated to the first preset temperature under conditions of temperature-pressure
Sludge disintegration is upper liquid and lower layer's pug；
The catalytic oxidizing equipment 30, is provided with catalysis oxidation area 304, for making the upper liquid in the catalysis oxidation
Area 304 and air effect generate oxidation solution, and the temperature for inputting the air in the catalysis oxidation area 304 is the second preset temperature；
The ammonia removal device 40 generates deamination tail washings, institute for the oxidation solution after cooling down with except ammonia pharmacy effect
The ammonia nitrogen concentration for stating deamination tail washings is lower than the ammonia nitrogen concentration of the oxidation solution；
The call-back device 50 generates relief liquor, the relief liquor for acting on the deamination tail washings and pH adjusting agent
PH value be specified pH value.
In the present embodiment, biochemical sludge to be processed is in pureed, 97% or more water content.Biochemical sludge is most due to moisture
It concentrates in the cell membrane film of microorganism, free water content is less, causes moisture separation difficult.But in certain hot conditions
Under, the cell wall rupture in biochemical sludge, the moisture in cell membrane can parse, and be converted into free water.In the process of heating
In, carbonization phenomenon can occur for organic matter in biochemical sludge, and the sludge after carbonization is changed into high concentrated organic wastewater (i.e. upper layer
Liquid) and a small amount of solid residue.It is flammable carbon block that carbonisation, which generates solid residue, can do fuel recovery utilization.High concentration
Organic wastewater imports catalysis oxidizing tower and makees oxidant using high hot-air, high concentration has using medium temperature catalytic wet oxidation technique
With the oxygen in air oxidation reaction occurs for machine waste water under the action of catalyst, and macromolecule contaminant is degraded, while most organic
Object is removed after depth degradation mineralising.In catalytic oxidation process, the oxidation reaction of generation can generate heat, and improving high concentration has
The temperature of machine waste water compensates for the thermal loss of catalytic oxidizing equipment 30.
DCS control system can be used in biochemical sludge processing system.DCS control system refers to dcs, again
Claim Distributed Control System.The mode that continuous feed can be used in biochemical sludge processing system handles biochemical sludge.
Specifically, heating device 10 is preprocessing module in biochemical sludge processing system, for biochemistry to be processed is dirty
Mud is heated to the first preset temperature.Multi-stage heat exchanger has can be set in heating device 10.Afterheat heat exchanger can be used in front end,
It is such as the afterheat heat exchanger of reacted oxidation solution using heat source；Heat exchanger in rear end can be compensation heat exchanger, so that
Biochemical sludge is heated to the first preset temperature.Compensation heat exchanger can use external conduction oil for heat source.First preset temperature can
To be 160-250 DEG C.Biochemical sludge can be heated to 60-70 DEG C from initial temperature, greatly using afterheat heat exchanger according to measuring and calculating
Energy consumption is saved greatly.In heating device 10, pressurizing device, such as force (forcing) pump can be set.Pressurizing device can be set in
Between afterheat heat exchanger and compensation heat exchanger.Pressurizing device can be 2-4MPa to the pressure that sludge applies.
Carbonizing plant 20, under conditions of temperature-pressure decomposing, the biochemical sludge for being heated to the first preset temperature
For upper liquid and lower layer's pug.In carbonizing plant 20, having heaters is set, for maintaining the carburizing temperature in device, so that
Carburizing reagent occurs during heating for biochemical sludge, forms upper liquid and lower layer's pug containing solid residue.It is filled in carbonization
It sets in 20, is additionally provided with separated structure, for separating upper liquid and lower layer's pug.It can be fixed according to the needs of practical operation technique
Carbonizing plant 20 is discharged in lower layer's pug by the phase.Lower layer's pug after filtering, can get filtrate and solid residue (i.e. flammable carbon
Block).Filtrate is reflowable to heating device 10, to continue carbonization treatment.
Catalytic oxidizing equipment 30 is provided with catalysis oxidation area 304, for making upper liquid in catalysis oxidation area 304 and air
Effect generates oxidation solution.Wherein, the temperature for the air for inputting catalysis oxidation area 304 is the second preset temperature.Second preset temperature
It can be 200-250 DEG C.In catalytic oxidizing equipment 30, the upper liquid of high concentration COD will continue in catalysis oxidation area 304 by oxygen
Change.Catalysis oxidation area 304 can be selected homogeneous and heterogeneous fixed bed and carry out catalysis oxidation, preferably heterogeneous fixation to upper liquid
Bed.Heterogeneous fixed bed can secondary pollution to avoid extra catalyst to aftertreatment device.The work of catalytic oxidizing equipment 30
It can be 160-250 DEG C as temperature, operating pressure can be 1.5-3.5MPa.In catalytic oxidizing equipment 30, organic matter is dropped
Solution, most of to be removed by thorough mineralising, organic nitrogen is changed into ammonia nitrogen.
The oxidation solution that catalytic oxidizing equipment 30 generates can flow into ammonia removal device 40 after decrease temperature and pressure.Ammonia removal device 40,
It is lower than oxidation solution with ammonia pharmacy effect, the ammonia nitrogen concentration of generation deamination tail washings, deamination tail washings is removed for the oxidation solution after cooling down
Ammonia nitrogen concentration.Here, except ammonia medicament may include lye and coagulant.In ammonia removal device 40, the pH value of oxidation solution will
It is adjusted to 11-14.Ammonia removal device 40 is additionally provided with ammonia and brushes device, removes ammonia for stripping.Meanwhile ammonia removal device 40 also connects
It is connected to gas absorbing device, for absorbing the ammonia in the tail gas after brushing except ammonia.After the processing of ammonia removal device 40, generation is removed
The ammonia nitrogen concentration of ammonia tail washings will substantially reduce.
Call-back device 50 generates relief liquor, the pH value of relief liquor is specified for acting on deamination tail washings and pH adjusting agent
PH value.Here, pH adjusting agent can refer to acid solution, such as hydrochloric acid.Specified pH value can be 7-8.Relief liquor after processing can return
It flow to biochemical conditioning tank (generating the processing pond of biochemical sludge).
Compared with prior art, biochemical sludge processing system provided in an embodiment of the present invention, in temperature-pressure and catalysis
Under the conditions of, biochemical sludge is changed into the relief liquor and carbonized residue of easy biochemical degradation by organic matter in efficient degradation sludge, dirty
Mud minimizing, innoxious, Treatment of Sludge is thorough, and cost is relatively low for integrated treatment.
Optionally, as shown in Fig. 2, the heating device 10 includes sequentially connected medicament adding unit 101, preheating unit
102 and reheating unit 103；The catalytic oxidizing equipment 30 includes heat recovery unit 301；
The medicament adding unit 101, for thermal oxide auxiliary agent to be added in the biochemical sludge by specified proportion；
There are heat transfers between the preheating unit 102 and the heat recovery unit 301；The preheating unit 102,
For absorbing heat, the heating biochemical sludge that thermal oxide auxiliary agent has been added from the heat recovery unit 301；The heat
Recovery unit 301 reduces the oxidation for the heat of the oxidation solution before cooling to be supplied to the preheating unit 102
The temperature of liquid；
The reheating unit 103 makes institute for heating to the biochemical sludge after the preheating unit 102 heating
It states biochemical sludge and reaches first preset temperature.
In the present embodiment, heating device 10 includes sequentially connected medicament adding unit 101, preheating unit 102 and reheating
Unit 103.Wherein, medicament adding unit 101 includes medicament adding device, thermal oxide auxiliary agent can be added by specified proportion biochemical
In sludge.Thermal oxide auxiliary agent can be hydrogen peroxide, sodium hypochlorite, at least one of concentrated sulfuric acid.The addition of thermal oxide auxiliary agent, one
Aspect can reduce the stickiness of sludge, on the other hand improving the mobility of its conveying then facilitates sludge in carbonizing plant 20
Carry out carburizing reagent.
The preheating unit 102 of heating device 10 can refer to the part that cold fluid flow passes through in afterheat heat exchanger.Catalysis oxidation dress
Hot fluid flows through in afterheat heat exchanger part can be referred to by setting 30 heat recovery unit 301.It is biochemical due to the reason of heat exchange
Sludge is after preheating unit 102, and temperature will increase, and oxidation solution is after heat recovery unit 301, and temperature will drop
It is low.High pressure tubular heat exchanger, such as tubular heat exchanger, movable tube sheets heat exchanger or double pipe heat exchanger can be selected in afterheat heat exchanger.
In some cases, the high-temperature tail gas of the generation of catalytic oxidizing equipment 30 also can be used as heat source in afterheat heat exchanger.
Reheating unit 103 reaches biochemical sludge for heating to the biochemical sludge after the heating of preheated unit 102
To the first preset temperature.After preheated unit 102 heats, biochemical sludge heating, but fail to reach the into carbonizing plant 20
One preset temperature.At this time, it may be necessary to provide additional heat to biochemical sludge, the first preset temperature is reached.Likewise, reheating list
Member 103 can also select high pressure tubular heat exchanger, and heat source can select high-temperature hot oil.
Optionally, as shown in figure 3, the carbonizing plant 20 includes carbonization sedimentation tower 203, the carbonization sedimentation tower 203 is wrapped
Include tower body, feed inlet 201, top discharge mouth 202, lower discharge port 204；
The feed inlet 201 is set in the middle part of tower body, and the biochemical sludge flows into the tower body from the feed inlet 201
Portion；
Inside the tower body, the top in the feed inlet 201, which is provided with, blocks mud inclined plate 207；
The top discharge mouth 202 is set at the top of the tower body, for the upper liquid to be discharged；
The lower discharge port 202 is set to the tower body bottom, for lower layer's pug to be discharged；
The lower discharge port 202 is connected with pug discharging adapter tube, pug discharging solenoid valve 205 in turn and by material container 206.
In the present embodiment, carbonizing plant 20 can be carbonization sedimentation tower 203.The sedimentation tower 203 that is carbonized includes tower body, feed inlet
201, top discharge mouth 202, lower discharge port 204.Feed inlet 201 is set in the middle part of tower body, and biochemical sludge flows into tower from feed inlet 201
Internal portion.The feeding manner of biochemical sludge can be continuous feed.Inside tower body, the top in feed inlet 201 is provided with
Block mud inclined plate 207.The number of plies for blocking mud inclined plate 207 can be multilayer.Top discharge mouth 202 is set at the top of tower body, for being discharged
Layer liquid.Lower discharge port 204 is set to tower body bottom, for lower layer's pug to be discharged.Lower discharge port 204 is connected with pug discharging in turn
Adapter tube, pug discharging solenoid valve 205 and by material container 206.Pug discharging solenoid valve 205 can refer to high pressure blowoff electromagnetic valve, and
It is connect with autocontrol switch, lower layer's pug is periodically discharged.By material container 206 for accommodating lower layer's pug.
Optionally, as shown in figure 4, catalytic oxidizing equipment 30 includes catalysis oxidizing tower 305, catalysis oxidizing tower 305 is provided with
Gas-liquid feed inlet 303 and oxidation solution discharge port 302, catalysis oxidation area 304304 are set to inside the tower body of catalysis oxidizing tower 305,
Gas-liquid feed inlet 303 is set to the bottom of catalysis oxidizing tower 305, and oxidation solution discharge port is set to the top of catalysis oxidizing tower 305.
The upper liquid flowed out from the top discharge mouth of carbonization sedimentation tower 203 and the compressed air for being previously heated to 200-250 DEG C
After mixing, catalysis oxidizing tower 305 is entered by gas-liquid feed inlet 303.In catalysis oxidation area 304304, in the effect of catalyst
Under, upper liquid generates oxidation solution by the dioxygen oxidation in air.Appropriate catalyst can be selected according to actual needs.
Optionally, the catalytic oxidizing equipment 30 further includes gas-liquid separator (not shown), the gas-liquid separator and institute
The connection of oxidation solution discharge port 302 is stated, the gas-liquid separator is for separating oxidation solution and by the input catalysis oxidation
The tail gas that the air in area 304 generates.
In the present embodiment, oxidation solution discharge port 302 can be connect with gas-liquid separator.After gas-liquid separator separates, it will obtain
Obtain oxidation solution and tail gas.The temperature of oxidation solution and tail gas is higher at this time, can separately flow into heat recovery unit 301 (referred to not
Same afterheat heat exchanger) heat recovery is carried out, reduce system energy consumption.
Optionally, the ammonia removal device 40 includes decompressor, dosing reactor tank, filter device；
The decompressor is provided with decompression input end and relief outlet end, the decompression input end and the heat recovery
Unit 301 connects；
The dosing reactor tank is provided with oxidation solution entrance, except ammonia medicament entrance and reaction solution export, the relief outlet
End is connect with the oxidation solution entrance；
The filter device includes filtering entrance and filtrate (liquid, and the filtering entrance and reaction solution outlet connect.
In the present embodiment, ammonia removal device 40 is provided with decompressor.Decompressor can be multi-step pressure reducing apparatus, make to aoxidize
The pressure of liquid is down to normal pressure.In dosing reactor tank with except ammonia medicament reacts, generation ammonia (dissolves oxidation solution after decrease temperature and pressure
In oxidation solution) and sediment (under the action of coagulant, being generated with the material effect in oxidation solution).At filter device
Reason, isolates filtrate and sediment.Filter device can be flame filter press.
Optionally, as shown in figure 5, ammonia removal device 40 further includes flash evaporation deamination tower 406, flash evaporation deamination tower 406 is provided with filter
Liquid import 401, liquid distributor 4011, the first air inlet 402, the second air inlet 403, the first gas distribution pipe 4021, the second gas distribution pipe
4031, packed bed 407, tail washings outlet 405 and deamination exhaust outlet 404；
Filtrate import 401 is set to the middle and upper part of 406 tower body of flash evaporation deamination tower, and outside connect with filtrate (liquid, inside and
The liquid distributor 4011 inside tower body is set to connect；
First air inlet 402, the second air inlet 403 are respectively arranged at the middle and lower part of 406 tower body of flash evaporation deamination tower, first into
402 inside of port is connect with the first gas distribution pipe 4021 being set to inside tower body, inside the second air inlet 403 and is set to tower body
Internal the second gas distribution pipe 4031 connection；
Top in the first gas distribution pipe 4021 and the second gas distribution pipe 4031, the lower section of liquid distributor 4011 are provided with filler
Bed 407；
Tail washings outlet 405 is set to the bottom of flash evaporation deamination tower 406；
Deamination exhaust outlet 404 is set to the top of flash evaporation deamination tower 406.
In the present embodiment, filtrate enters in flash evaporation deamination tower 406 from filtrate import 401, is uniformly sprayed by liquid distributor 4011
It shines on the packing layer in tower.The tail gas that gas-liquid separator generates can be passed through in the first gas distribution pipe 4021 from the first air inlet 402,
The cold air of compensation can be passed through in the second gas distribution pipe 4031 from the second air inlet 403, the ammonia contained in stripping filtrate.After stripping
Gas from deamination exhaust outlet 404 be discharged.And the filtrate (i.e. deamination tail washings) after deamination is flowed out from tail washings outlet 405.
It optionally, further include ammonia absorption device, the ammonia absorption device is connect with the deamination exhaust outlet 404.
In the present embodiment, due to containing ammonia in tail gas, tail gas need to be carried out to prevent pollution atmosphere except ammonia treatment.Ammonia
Spray equipment has can be set in absorption plant, is recycled using water or dilute sulfuric acid to ammonia, formed corresponding ammonia spirit and
Ammonium sulfate.
Optionally, the call-back device 50 includes pH conditioning tank, pH tester and soda acid chemicals dosing plant；
The pH conditioning tank, for accommodating the deamination tail washings；
The pH tester, for measuring the pH value of liquid in the pH conditioning tank；
The soda acid chemicals dosing plant, for the pH adjusting agent to be added toward the pH conditioning tank.
In this implementation, deamination tail washings is flowed into pH conditioning tank, and pH tune is then added in soda acid chemicals dosing plant into pH conditioning tank
Agent is saved, the pH value of deamination tail washings is adjusted.PH tester then can be used for judging whether the pH value of the filtrate after adjusting is up to standard.Herein
Place, pH adjusting agent can be diluted acid, such as dilute sulfuric acid or dilute hydrochloric acid.If the pH value of the filtrate after adjusting is up to standard (at this point, pH value is
7-8), then the filtrate (as relief liquor) after adjusting can be emitted into biochemical conditioning tank.
As shown in fig. 6, the embodiment of the invention also provides a kind of biochemical sludge processing methods, comprising:
S10, biochemical sludge to be processed is heated to the first preset temperature；
S20, under the conditions of preset temperature-pressure, be decomposed into the biochemical sludge for being heated to the first preset temperature
Layer liquid and lower layer's pug；
S30, so that the upper liquid is carried out catalysed oxidn under the second preset temperature, generate oxidation solution；
S40, by decrease temperature and pressure device to the oxidation solution decrease temperature and pressure, by after decrease temperature and pressure the oxidation solution with
Except ammonia medicament reacts, deamination tail washings is generated, the ammonia nitrogen concentration of the deamination tail washings is lower than the ammonia nitrogen concentration of the oxidation solution；
S50, it reacts the deamination tail washings with pH adjusting agent, generates relief liquor, the pH value of the relief liquor is specified pH
Value.
The specific processing step of biochemical sludge processing method can refer to the description of an embodiment biochemical sludge processing system,
Details are not described herein.
Application example 1
Certain medium-sized municipal sewage plant, day handle 200,000 tons of city domestic sewage, produce remaining 120 tons of biochemical sludge daily,
Former treatment process is squeezed biochemical sludge to after aqueous 75% using mud snail machine, is transported to cement plant nearby outside and is handled into kiln collaboration.
After biochemical sludge processing system provided by the invention processing, no outward transport sludge.It is formed daily after Treatment of Sludge and imports department of biochemistry
The relief liquor of system is 120 cubes, COD7000mg/L -8000mg/L, B/C=0.35-0.45, the limpid liquid of appearance greenish transparent
Body runs without influence, about 3 tons of carbon blocks of above-mentioned daily output biochemical system.After biochemical sludge processing system, at the sewage
It manages the annual operating cost of factory and reduces by 1000 Yu Wanyuan.
Application Example 2
Certain large-scale pesticide producing enterprise, biochemical sewage treating stations handle 2000 cubes of pesticide comprehensive wastewater daily.It produces daily
3 tons of biochemical sludge out form 2.5 tons of dangerous wastes daily after compression, need to send hazardous waste center incineration disposal.It provides according to the present invention
The skid-mounted type integrated equipment that biochemical sludge processing system is built, directly applies in biochemical sewage treating stations, and biochemical sludge is turned
Turn to relief liquor.The relief liquor COD of formation is no more than 10000mg/L, B/C=0.38, and relief liquor returns to factory's biochemical treatment tune
Section processing.After transformation, environmentally friendly operating cost reduces about 3,000,000 yuan to biochemical sewage treating stations every year.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Made any modifications, equivalent replacements, and improvements etc., should all be included in the protection scope of the present invention within mind and principle.
Claims (10)
1. a kind of biochemical sludge processing system, which is characterized in that including sequentially connected heating device, carbonizing plant, catalysis oxygen
Makeup sets, ammonia removal device and call-back device；
The heating device, for biochemical sludge to be processed to be heated to the first preset temperature；
The carbonizing plant, the biochemical sludge point under conditions of temperature-pressure, making to be heated to the first preset temperature
Solution is upper liquid and lower layer's pug；
The catalytic oxidizing equipment is provided with catalysis oxidation area, for making the upper liquid in the catalysis oxidation area and air
Effect generates oxidation solution, and the temperature for inputting the air in the catalysis oxidation area is the second preset temperature；
The ammonia removal device generates deamination tail washings, the deamination for the oxidation solution after cooling down with except ammonia pharmacy effect
The ammonia nitrogen concentration of tail washings is lower than the ammonia nitrogen concentration of the oxidation solution；
The call-back device generates relief liquor, the pH value of the relief liquor for acting on the deamination tail washings and pH adjusting agent
To specify pH value.
2. biochemical sludge processing system as described in claim 1, which is characterized in that the heating device includes sequentially connected
Medicament adding unit, preheating unit and hot cell again；The catalytic oxidizing equipment includes heat recovery unit；
The medicament adding unit, for thermal oxide auxiliary agent to be added in the biochemical sludge by specified proportion；
There are heat transfers between the preheating unit and the heat recovery unit；The preheating unit is used for from the heat
It measures recovery unit and absorbs heat, the heating biochemical sludge that thermal oxide auxiliary agent has been added；The heat recovery unit, being used for will
The heat of the oxidation solution before cooling is supplied to the preheating unit, reduces the temperature of the oxidation solution；
The hot cell again makes the biochemical sludge for heating to the biochemical sludge after preheating unit heating
Reach first preset temperature.
3. biochemical sludge processing system as described in claim 1, which is characterized in that the carbonizing plant includes carbonization sedimentation
Tower, the carbonization sedimentation tower include tower body, feed inlet, top discharge mouth, lower discharge port；
The feed inlet is set in the middle part of tower body, and the biochemical sludge flows into inside the tower body from the feed inlet；
Inside the tower body, it is provided with above the feed inlet and blocks mud inclined plate；
The top discharge mouth is set at the top of the tower body, for the upper liquid to be discharged；
The lower discharge port is set to the tower body bottom, for lower layer's pug to be discharged；
The lower discharge port is connected with pug discharging adapter tube, pug discharging solenoid valve in turn and by material container.
4. biochemical sludge processing system as described in claim 1, which is characterized in that the catalytic oxidizing equipment includes catalysis oxygen
Change tower, the catalysis oxidizing tower is provided with gas-liquid feed inlet and oxidation solution discharge port, and the catalysis oxidation area is set to described urge
Inside the tower body for changing oxidizing tower, the gas-liquid feed inlet is set to the bottom of the catalysis oxidizing tower, the oxidation solution discharge port
It is set to the top of the catalysis oxidizing tower.
5. biochemical sludge processing system as claimed in claim 4, which is characterized in that the catalytic oxidizing equipment further includes gas-liquid
Separator, the gas-liquid separator are connect with the oxidation solution discharge port, the gas-liquid separator for separate oxidation solution and
The tail gas generated by the air in the input catalysis oxidation area.
6. biochemical sludge processing system as claimed in claim 2, which is characterized in that the ammonia removal device include decompressor,
Dosing reactor tank, filter device；
The decompressor is provided with decompression input end and relief outlet end, the decompression input end and the heat recovery unit
Connection；
The dosing reactor tank is provided with oxidation solution entrance, except ammonia medicament entrance and reaction solution export, the relief outlet end with
The oxidation solution entrance connection；
The filter device includes filtering entrance and filtrate (liquid, and the filtering entrance and reaction solution outlet connect.
7. biochemical sludge processing system as claimed in claim 6, which is characterized in that the ammonia removal device further includes flash evaporation deamination
Tower, the flash evaporation deamination tower are provided with filtrate import, liquid distributor, the first air inlet, the second air inlet, the first gas distribution pipe, second
Gas distribution pipe, packed bed, tail washings outlet and deamination exhaust outlet；
The filtrate import is set to the middle and upper part of the flash evaporation deamination tower tower body, external to connect with the filtrate (liquid, internal
It is connect with the liquid distributor being set to inside tower body；
First air inlet, the second air inlet are respectively arranged at the middle and lower part of the flash evaporation deamination tower tower body, described first into
It connect inside port with first gas distribution pipe being set to inside tower body, inside second air inlet and is set in tower body
Second gas distribution pipe in portion connects；
Top in first gas distribution pipe and second gas distribution pipe, the lower section of the liquid distributor are provided with the filler
Bed；
The tail washings outlet is set to the bottom of the flash evaporation deamination tower；
The deamination exhaust outlet is set to the top of the flash evaporation deamination tower.
8. biochemical sludge processing system as claimed in claim 7, which is characterized in that it further include ammonia absorption device, the ammonia
Aspiration receiving apparatus is connect with the deamination exhaust outlet.
9. biochemical sludge processing system as described in claim 1, which is characterized in that the call-back device include pH conditioning tank,
PH tester and soda acid chemicals dosing plant；
The pH conditioning tank, for accommodating the deamination tail washings；
The pH tester, for measuring the pH value of liquid in the pH conditioning tank；
The soda acid chemicals dosing plant, for the pH adjusting agent to be added toward the pH conditioning tank.
10. biochemical sludge processing method characterized by comprising
Biochemical sludge to be processed is heated to the first preset temperature；
Under the conditions of preset temperature-pressure, the biochemical sludge for being heated to the first preset temperature is made to be decomposed into upper liquid under
Layer pug；
So that the upper liquid is carried out catalysed oxidn under the second preset temperature, generates oxidation solution；
By decrease temperature and pressure device to the oxidation solution decrease temperature and pressure, by the oxidation solution after decrease temperature and pressure and ammonia medicament is removed
Reaction, generates deamination tail washings, and the ammonia nitrogen concentration of the deamination tail washings is lower than the ammonia nitrogen concentration of the oxidation solution；
It reacts the deamination tail washings with pH adjusting agent, generates relief liquor, the pH value of the relief liquor is specified pH value.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910372302.4A CN110078326B (en) | 2019-05-06 | 2019-05-06 | Biochemical sludge treatment system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910372302.4A CN110078326B (en) | 2019-05-06 | 2019-05-06 | Biochemical sludge treatment system and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110078326A true CN110078326A (en) | 2019-08-02 |
| CN110078326B CN110078326B (en) | 2024-03-19 |
Family
ID=67418914
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910372302.4A Active CN110078326B (en) | 2019-05-06 | 2019-05-06 | Biochemical sludge treatment system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110078326B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101134607A (en) * | 2006-08-29 | 2008-03-05 | 北京索能技术有限公司 | Method and device for flash evaporation deamination |
| CN105152446A (en) * | 2015-09-25 | 2015-12-16 | 浙江奇彩环境科技有限公司 | Treatment process for acesulfameK production wastewater |
| CN105307986A (en) * | 2013-05-03 | 2016-02-03 | 得利满公司 | Method for ultra-dehydrating thickened or pasty biomass products, and equipment for implementing the method |
| CN106746135A (en) * | 2017-03-09 | 2017-05-31 | 江苏省环境科学研究院 | The processing system and technique of a kind of N-(phosphonomethyl) iminodiacetic acid wastewater |
| CN109477011A (en) * | 2016-06-23 | 2019-03-15 | C-绿色科技公司 | Method for liquid phase oxidation in hydrothermal carbonization technique |
| CN210085221U (en) * | 2019-05-06 | 2020-02-18 | 姜林 | Biochemical sludge treatment system |
-
2019
- 2019-05-06 CN CN201910372302.4A patent/CN110078326B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101134607A (en) * | 2006-08-29 | 2008-03-05 | 北京索能技术有限公司 | Method and device for flash evaporation deamination |
| CN105307986A (en) * | 2013-05-03 | 2016-02-03 | 得利满公司 | Method for ultra-dehydrating thickened or pasty biomass products, and equipment for implementing the method |
| CN105152446A (en) * | 2015-09-25 | 2015-12-16 | 浙江奇彩环境科技有限公司 | Treatment process for acesulfameK production wastewater |
| CN109477011A (en) * | 2016-06-23 | 2019-03-15 | C-绿色科技公司 | Method for liquid phase oxidation in hydrothermal carbonization technique |
| CN106746135A (en) * | 2017-03-09 | 2017-05-31 | 江苏省环境科学研究院 | The processing system and technique of a kind of N-(phosphonomethyl) iminodiacetic acid wastewater |
| CN210085221U (en) * | 2019-05-06 | 2020-02-18 | 姜林 | Biochemical sludge treatment system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110078326B (en) | 2024-03-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104030427B (en) | Supercritical water oxidation treatment system for printing and dyeing wastewater and sludge | |
| CN101979349B (en) | Tubular pyrohydrolysis treatment method and device for sludge | |
| CN102992559B (en) | Method for comprehensively utilizing anaerobic digestion and carbonization of municipal sludge | |
| CN103819044B (en) | A kind of compound transformation catalysis oxidation high-concentration organic wastewater treatment system of magnetic strength ultraviolet light microwave and method | |
| CN101993143B (en) | System and method for treating caustic sludge wastewater by using supercritical water oxidation method | |
| CN105967490A (en) | Method and continuous system for treating wet organic waste | |
| CN102234170A (en) | Method and device for rapidly reducing moisture content of sludge | |
| CN105254146A (en) | Supercritical water oxidation treatment system and technology for dyeing sludge | |
| CN105601017A (en) | Near zero emission treatment system and method for high-concentration organic wastewater and sludge | |
| CN106145574A (en) | A kind of multi-section tube type mud Rapid Thermal hydrolysis process technique | |
| CN206607136U (en) | A kind of sludge water thermal oxidative reaction system for pretreatment of being backflowed with product | |
| CN106830469A (en) | VUV photo catalysis reactor, wastewater treatment equipment and processing method | |
| CN104496004A (en) | High-concentration organic pesticide wastewater supercritical water oxidation treatment system and method | |
| CN108751653B (en) | Supercritical water oxidation staged oxidation treatment system and process for municipal sludge | |
| CN101774739A (en) | Treatment technology for wastewater from production of neopentyl glycol | |
| CN105502842A (en) | Wastewater Fenton oxidation-biological combined treatment method and device capable of recycling sludge | |
| CN108383335A (en) | High-concentration organic wastewater treatment system and method | |
| CN205803293U (en) | A kind of continuous way processing system of wet matter organic waste | |
| CN210085221U (en) | Biochemical sludge treatment system | |
| CN100432530C (en) | Internal combustion circulating energy conversion system for supercritical oxidation | |
| CN110078326A (en) | Biochemical sludge processing system and method | |
| CN208829523U (en) | A kind of waste plastic and municipal sludge co-oxidation processing unit | |
| CN113045082A (en) | Intelligent treatment system and method for PMIDA high-salinity wastewater | |
| CN105692951B (en) | The waste water iron-carbon reduction processing method and its device that a kind of iron cement recycles | |
| CN214528484U (en) | Normal temperature processing system of high ammonia-nitrogen wastewater with low carbon-nitrogen ratio |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |