CN114804557A - Method for utilizing sludge in-situ micro-channel carbon source - Google Patents
Method for utilizing sludge in-situ micro-channel carbon source Download PDFInfo
- Publication number
- CN114804557A CN114804557A CN202210509714.XA CN202210509714A CN114804557A CN 114804557 A CN114804557 A CN 114804557A CN 202210509714 A CN202210509714 A CN 202210509714A CN 114804557 A CN114804557 A CN 114804557A
- Authority
- CN
- China
- Prior art keywords
- sludge
- carbon source
- slurry
- sewage
- utilizing
- 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.)
- Withdrawn
Links
Images
Classifications
-
- 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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
-
- 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
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
Abstract
A method for utilizing sludge in situ micro-channel carbon source comprises the steps of carrying out viscosity reduction treatment on sludge, then pyrolyzing the sludge by using a micro-channel sludge in situ carbon source device two-stage reactor, increasing the heating area of the sludge under the condition of the same heat source, improving the pyrolysis efficiency, and thoroughly decomposing sludge microbial protein to generate substances such as acetate, fat decomposition products, saccharides and the like; adding an ammonia nitrogen remover into the pyrolyzed slurry to convert ammonia nitrogen groups in amino acid substances into nitrogen under the action of the ammonia nitrogen remover, or hydrolyzing the ammonia nitrogen groups into hydroxyl groups, nitro groups and the like, so that the content of ammonia nitrogen in the sludge degradation liquid is reduced, and the sludge degradation liquid can be used as a carbon source for a sewage nitrogen and phosphorus removal system; meanwhile, the existing devices of sewage plants are fully utilized to carry out deep harmless treatment on the degraded sludge, so that the equipment investment and the treatment cost of the deep treatment of the sludge can be greatly reduced, and the method has remarkable social and economic benefits.
Description
Technical Field
The invention relates to a method for utilizing a carbon source in a sludge in-situ micro-channel, belonging to the technical field of sludge resource treatment and utilization.
Background
The COD concentration of inlet water of domestic sewage treatment plants in China is low, the C/N in sewage is low, and a carbon source is lacked in the denitrification process. In order to achieve the standard discharge of sewage, the sewage treatment plant usually adopts an external carbon source (such as methanol, acetic acid, glucose and the like) to solve the problem, so that the operation cost of the sewage treatment plant is increased, the sludge yield is increased, and the sludge treatment is always a troublesome problem in the environmental protection industry.
The content of organic matters in the residual sludge generated by sewage treatment is about 60 percent, the content of biodegradable organic components is more than 40 percent, and the biodegradable organic matters mainly comprise protein, polysaccharide and the like, can be hydrolyzed and acidified under certain conditions and are converted into a carbon source-Volatile Fatty Acid (VFA) which can be utilized by organisms. Meanwhile, in a biological nitrogen and phosphorus removal system for sewage, carbon sources are consumed in the processes of denitrification, phosphorus release of phosphorus accumulating bacteria, anaerobic bacteria self metabolism and the like, and the type of the carbon sources has direct influence on the biodegradability of the carbon sources, so that the denitrification rate is influenced.
Temperature is an important factor influencing the hydrolytic acidification reaction of the sludge, on one hand, the activity of intracellular and extracellular enzymes of the hydrolytic acidification bacteria is influenced, so that the metabolic rate of the hydrolytic acidification bacteria is influenced, and on the other hand, the high temperature can break cell walls and hydrolyze proteins, so that intracellular substances are released. Due to the fact that the temperature of the pyrolysis treatment technology is high, the design and construction requirements of the currently adopted sludge pyrolysis tank or reaction tank are high, the interior of the current process equipment is mostly designed in an integrated mode, and the problems of uneven heating and low pyrolysis efficiency exist. In addition, the sludge production amount is large, the water content is high, the transportation cost of the ex-situ treatment is large, and the actual popularization and application of the existing sludge ex-situ treatment technology and equipment are limited.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method for utilizing sludge in situ by using a microchannel carbon source, namely, after viscosity reduction treatment is carried out on the sludge, a microchannel sludge in situ carbon source device is used for pyrolyzing the sludge, so that sludge microbial protein is thoroughly decomposed to generate substances such as acetate, fat decomposition products, saccharides and the like, and the substances are used as a carbon source for a sewage nitrogen and phosphorus removal system.
The invention comprises the following steps:
(1) conveying the sludge into a double-shaft stirrer through a metering screw, adding a pre-viscosity reducer and a viscosity reducer into the front section and the middle section of the stirrer in sequence, controlling the slurry to flow out by using an overflow baffle, and allowing the slurry overflowing from the middle section to enter a tail section buffer tank;
(2) the viscosity reduction slurry flowing out of the buffer tank of the stirrer is respectively conveyed to tube sides of a first-stage reactor and a second-stage reactor of a micro-channel sludge in-situ carbonization device through a high-pressure pump; a heat source in the first-stage reactor goes through a shell pass, and the viscosity reduction slurry in a tube pass is subjected to pyrolysis treatment, so that microbial chemical substances in the viscosity reduction slurry are subjected to wall breaking and dissolution;
(3) the pyrolysis slurry flowing out of the primary reactor enters a shell pass of the secondary reactor after an ammonia nitrogen remover is quantitatively added through a metering pump, and the viscosity reduction slurry in a tube pass of the secondary reactor is preheated, so that the heat energy utilization and ammonia nitrogen removal reaction of the pyrolysis slurry of the primary reactor are synchronously completed;
(4) pumping the preheated viscosity-reducing slurry flowing out of the tube side of the secondary reactor into the tube side of the primary reactor for pyrolysis treatment;
(5) the slurry degradation liquid flowing out of the shell pass of the secondary reactor is divided into a liquid phase and a slag phase by a centrifugal machine, the liquid phase mainly comprises substances such as substituted acetates, fat and fat decomposition products, saccharides and the like which are completely decomposed and deaminated by sludge microbial protein, and the substances are used as carbon sources for a sewage denitrification and dephosphorization system; the slag phase mainly comprises silt substances and flocculating agents such as phosphorus, iron, aluminum and the like contained in the original sludge, the mineralized slag is decomposed and is stable and harmless mechanical impurities, a part of liquid phase serving as a carbon source is carried in the slag phase, the material is sent to a water inlet unit of a sewage plant, enters a cyclone grit chamber through a grid tank, organic carbon source components carried in the slag phase are washed out by utilizing the elutriation effect of sewage and then enters a nitrogen and phosphorus removal system together with the sewage, and the elutriated and residual harmless silt mineralized slag is separated in the cyclone grit chamber and is further treated and utilized.
The micro-channel sludge in-situ carbon generation device is a combined micro-channel sludge in-situ pyrolysis carbonization device (application number: 2022210217289) or a self-stirring micro-channel sludge in-situ carbonization device (application number: 2022210217240) which is previously applied by the applicant, and if a primary reactor of the self-stirring micro-channel sludge in-situ carbon generation device is adopted, a heater is required to be arranged for heating pyrolysis liquid. Meanwhile, a valve between the double-shaft stirrer and the secondary reactor can be opened according to the process requirement, and whether the viscosity-reducing slurry flows into the secondary reactor or not is controlled.
The slurry degradation liquid flowing out of the shell pass of the secondary reactor can be directly sent into a water inlet unit of a sewage plant in the form of mixed liquid without separation, enters a cyclone grit chamber through a grid chamber, elutriates organic carbon source components in the mixed liquid by using the elutriation effect of sewage, then enters a nitrogen and phosphorus removal system along with the sewage, and elutriates residual harmless silt and mineralized slag to be separated in the cyclone grit chamber for further treatment and utilization.
The inner shell of the double-shaft stirrer adopts organic silicon resin, phenolic resin, epoxy resin or polyester resin for corrosion prevention.
The pre-viscosity reducer is H 2 SO 4 、HCl、HNO 3 One or more of the components, wherein the pH value is 1-3, and the addition amount is 0.1-1% of the volume percentage of the sludge.
The viscosity reducer is Ca (OH) 2 、MgO、CaO、Mg(OH) 2 、KMnO 4 One or more of the sludge is added in an amount of 0.5-2 g/L.
The ammonia nitrogen remover is H 2 O 2 、Ca(ClO) 2 One or more of NaClO and HClO, wherein the addition amount of the NaClO and the HClO is 1-3% of the volume percentage of the sludge.
The temperature of the pyrolysis treatment is 120-200 ℃, and the time of the pyrolysis treatment is 30-60 min.
The invention has the beneficial effects that:
(1) the invention adopts the sludge in-situ microchannel carbon source utilization device to carry out pyrolysis treatment on the sludge, increases the heating area of the sludge under the condition of the same heat source, improves the pyrolysis efficiency, leads the sludge microbial protein to be thoroughly decomposed to generate acetate, fat and fat decomposition products, organic matters easy to be biodegraded such as saccharides and the like, and is used as a carbon source to be reused in a sewage denitrification and dephosphorization system, thereby realizing the in-situ carbon source utilization of the sludge.
(2) Before the sludge enters the micro-channel carbon source utilization device, the viscosity reduction pretreatment is carried out on the sludge, and the floccule structure of the sludge is efficiently destroyed in stages, so that the conveying resistance of the sludge in the tube pass of the micro-channel carbon source utilization device is reduced, microorganisms in the floccule are exposed, and the pyrolysis of the sludge is facilitated to break the wall and dissolve out intracellular substances.
(3) According to the invention, an ammonia nitrogen remover is added into pyrolysis slurry flowing out of a primary reactor, so that ammonia nitrogen groups in amino acid substances are converted into nitrogen under the action of the ammonia nitrogen remover or hydrolyzed into hydroxyl, nitro and the like, and the content of ammonia nitrogen in the sludge degradation liquid serving as a carbon source is reduced.
(4) The sludge in-situ carbonization process fully utilizes the existing devices of sewage plants to carry out deep harmless treatment on the degraded sludge, can greatly reduce the equipment investment and treatment cost of sludge deep treatment, and has remarkable social and economic benefits.
Drawings
FIG. 1 is a process flow diagram of a method for utilizing sludge in situ micro-channel carbon source.
1. The system comprises a double-shaft stirrer, 2, a pre-viscosity reducer dosing device, 3, a viscosity reducer dosing device, 4, a high-pressure pump, 5, a micro-channel sludge in-situ carbonation device primary reactor, 6, a micro-channel sludge in-situ carbonation device secondary reactor, 7, a heater, 8, an ammonia nitrogen remover dosing device, 9, a centrifuge, 10, a sewage nitrogen and phosphorus removal system, 11, a grid tank, 12 and a rotational flow grit chamber.
DETAILED DESCRIPTION OF EMBODIMENT (S) OF INVENTION
The following examples are embodied in Tianjin sewage plant, and the sludge produced in the sewage treatment process of the sewage plant has a water content of about 90%.
Example 1
(1) Conveying the sludge to a double-shaft stirrer through a metering screw, adding sulfuric acid solution (pH = 2) with the volume percentage of 0.5% of the sludge at the front section of the stirrer, and adding Ca (OH) at the middle section of the stirrer 2 Powder, the addition amount of which is 0.5g/L sludge, the overflow baffle is utilized to control the slurry to flow out, and the slurry overflowed from the middle section enters a tail section buffer pool; the inner shell of the double-shaft stirrer is subjected to anti-corrosion treatment by adopting organic silicon resin;
(2) the viscosity reduction slurry flowing out of the buffer pool of the stirrer is conveyed to a first-stage reactor of a combined type microchannel sludge in-situ pyrolysis carbonization device (application number: 2022210217289) through a high-pressure pump, and after a shell pass of a second-stage reactor (which does not need to be electrified and heated) is filled with the slurry, a valve between the stirrer and the second-stage reactor is opened, so that the viscosity reduction slurry flows into a tube pass of the second-stage reactor; carrying out pyrolysis treatment on the viscosity reduction slurry in a tube pass by taking a heat source away from a shell pass in a primary reactor, controlling the pyrolysis temperature at 140 ℃, and keeping the pyrolysis time for about 35min to break the wall of the microbial chemical substances in the viscosity reduction slurry and dissolve out;
(3) adding H with the sludge volume percentage of 2 percent into the pyrolysis slurry flowing out of the primary reactor through a metering pump 2 O 2 Then, entering a shell pass of a secondary reactor, preheating viscosity-reducing slurry in a tube pass of the secondary reactor, and synchronously completing heat energy utilization and ammonia nitrogen elimination reaction of pyrolysis slurry of the primary reactor;
(4) pumping the preheated viscosity-reducing slurry flowing out of the tube side of the secondary reactor into the tube side of the primary reactor for pyrolysis treatment;
(5) separating slurry degradation liquid flowing out of a shell pass of the secondary reactor into a liquid phase and a slag phase through a centrifugal machine, wherein the dissolution rates of protein, soluble polysaccharide and SCOD in the liquid phase are respectively 51%, 60% and 59%, and TN =284mg/L, and the slurry degradation liquid is used as a carbon source to be reused in a sewage nitrogen and phosphorus removal system; the slag phase mainly comprises silt substances and flocculating agents such as phosphorus, iron, aluminum and the like contained in the original sludge, the mineralized slag is decomposed and is stable and harmless mechanical impurities, a part of liquid phase serving as a carbon source is carried in the slag phase, the material is sent to a water inlet unit of a sewage plant, enters a cyclone grit chamber through a grid tank, organic carbon source components carried in the slag phase are washed out by utilizing the elutriation effect of sewage and then enters a nitrogen and phosphorus removal system together with the sewage, and the elutriated and residual harmless silt mineralized slag is separated in the cyclone grit chamber and is further treated and utilized.
Example 2
(1) Conveying the sludge into a double-shaft stirrer through a metering screw, adding 0.7 volume percent hydrochloric acid (pH = 3) into the front section of the stirrer, and adding Mg (OH) into the middle section of the stirrer 2 Powder with the addition of 1.6g/L sludge, the overflow baffle is utilized to control the slurry to flow out, and the slurry overflowed from the middle section enters a tail section buffer pool; the inner shell of the double-shaft stirrer adopts phenolic aldehydePerforming corrosion prevention treatment on the resin;
(2) the viscosity reduction slurry flowing out of the buffer pool of the stirrer is conveyed to a self-stirring type micro-channel sludge in-situ carbonization device (application number: 2022210217240) through a high-pressure pump, and after the shell side of a secondary reactor is filled with the slurry, a valve between the stirrer and the secondary reactor is opened to ensure that the viscosity reduction slurry flows into the tube side of the secondary reactor; carrying out pyrolysis treatment on the viscosity reduction slurry in a tube pass by a heat source in a first-stage reactor, controlling the pyrolysis temperature at 190 ℃ and keeping the pyrolysis time for about 50min to break the wall of the microbial chemical substances in the viscosity reduction slurry and dissolve out;
(3) adding HClO with the sludge volume percentage of 3% into pyrolysis slurry flowing out of the primary reactor through a metering pump, then entering a shell pass of the secondary reactor, preheating viscosity reduction slurry in a tube pass of the secondary reactor, and synchronously completing heat energy utilization and ammonia nitrogen elimination reaction of the pyrolysis slurry of the primary reactor;
(4) the dissolution rates of protein, soluble polysaccharide and SCOD in the slurry degradation liquid flowing out of the shell pass of the secondary reactor are 82%, 79% and 86% respectively, TN =311mg/L, the slurry degradation liquid is directly sent into a water inlet unit of a sewage plant in the form of mixed liquid, the mixed liquid enters a rotational flow grit chamber through a grid chamber, organic carbon source components in the mixed liquid are washed out by the elutriation effect of sewage and then enter a nitrogen and phosphorus removal system together with the sewage, and the elutriated residual harmless silt and mineralized slag is separated in the rotational flow grit chamber for further treatment and utilization.
Although the preferred embodiments of the present invention have been described above with reference to the accompanying drawings, the present invention is not limited to the above-described embodiments, which are merely illustrative and not restrictive, and those skilled in the art can make many modifications without departing from the spirit and scope of the present invention as defined in the appended claims.
Claims (7)
1. A method for utilizing sludge in situ micro-channel carbon source comprises the following steps:
(1) conveying the sludge into a double-shaft stirrer through a metering screw, adding a pre-viscosity reducer and a viscosity reducer into the front section and the middle section of the stirrer in sequence, controlling the slurry to flow out by using an overflow baffle, and allowing the slurry overflowing from the middle section to enter a tail section buffer tank;
(2) the viscosity reduction slurry flowing out of the buffer tank of the stirrer is respectively conveyed to tube sides of a first-stage reactor and a second-stage reactor of a micro-channel sludge in-situ carbonization device through a high-pressure pump; a heat source in the first-stage reactor goes through a shell pass, and the viscosity reduction slurry in a tube pass is subjected to pyrolysis treatment, so that microbial chemical substances in the viscosity reduction slurry are subjected to wall breaking and dissolution;
(3) the pyrolysis slurry flowing out of the primary reactor enters a shell pass of the secondary reactor after an ammonia nitrogen remover is quantitatively added through a metering pump, and the viscosity reduction slurry in a tube pass of the secondary reactor is preheated, so that the heat energy utilization and ammonia nitrogen removal reaction of the pyrolysis slurry of the primary reactor are synchronously completed;
(4) pumping the preheated viscosity-reducing slurry flowing out of the tube side of the secondary reactor into the tube side of the primary reactor for pyrolysis treatment;
(5) the slurry degradation liquid flowing out of the shell pass of the secondary reactor is separated into a liquid phase and a slag phase through a centrifugal machine, and the liquid phase is used as a carbon source and is reused in a sewage nitrogen and phosphorus removal system; and (3) conveying a part of liquid phase which is taken as a carbon source in the slag phase into a water inlet unit of a sewage plant, feeding the liquid phase into a cyclone grit chamber through a grid tank, washing out organic carbon source components carried in the slag phase by utilizing the elutriation effect of sewage, feeding the organic carbon source components and the sewage into a nitrogen and phosphorus removal system, and separating the elutriated and residual harmless silt and mineralized slag in the cyclone grit chamber for further treatment and utilization.
2. The method for utilizing the sludge in the in-situ micro-channel carbon source as claimed in claim 1, wherein: the inner shell of the double-shaft stirrer adopts organic silicon resin, phenolic resin, epoxy resin or polyester resin for corrosion prevention.
3. The method for utilizing the sludge in the in-situ micro-channel carbon source as claimed in claim 1, wherein: the pre-thinning agent is H 2 SO 4 、HCl、HNO 3 One or more of them, pH is 1-3, and the addition amount isIs 0.1-1% of the sludge volume percentage.
4. The method for utilizing the sludge in the in-situ micro-channel carbon source as claimed in claim 1, wherein: the viscosity reducer is Ca (OH) 2 、MgO、CaO、Mg(OH) 2 、KMnO 4 One or more of the sludge is added in an amount of 0.5-2 g/L.
5. The method for utilizing the sludge in the in-situ micro-channel carbon source as claimed in claim 1, wherein: the ammonia nitrogen remover is H 2 O 2 、Ca(ClO) 2 One or more of NaClO and HClO, wherein the addition amount of the NaClO and the HClO is 1-3% of the volume percentage of the sludge.
6. The method for utilizing the sludge in situ micro-channel carbon source as claimed in claims 1 and 5, wherein: the temperature of the pyrolysis treatment is 120-200 ℃, and the time of the pyrolysis treatment is 30-60 min.
7. The method for utilizing the sludge in situ micro-channel carbon source as claimed in claims 1 and 5, wherein: the slurry degradation liquid flowing out of the shell pass of the secondary reactor can be directly sent into a water inlet unit of a sewage plant in the form of mixed liquid without separation, enters a cyclone grit chamber through a grid chamber, elutriates organic carbon source components in the mixed liquid by using the elutriation effect of sewage, then enters a nitrogen and phosphorus removal system along with the sewage, and elutriates residual harmless silt and mineralized slag to be separated in the cyclone grit chamber for further treatment and utilization.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210509714.XA CN114804557A (en) | 2022-05-11 | 2022-05-11 | Method for utilizing sludge in-situ micro-channel carbon source |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210509714.XA CN114804557A (en) | 2022-05-11 | 2022-05-11 | Method for utilizing sludge in-situ micro-channel carbon source |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114804557A true CN114804557A (en) | 2022-07-29 |
Family
ID=82513425
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210509714.XA Withdrawn CN114804557A (en) | 2022-05-11 | 2022-05-11 | Method for utilizing sludge in-situ micro-channel carbon source |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114804557A (en) |
-
2022
- 2022-05-11 CN CN202210509714.XA patent/CN114804557A/en not_active Withdrawn
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20200062628A1 (en) | Bioreactor for treating sewage and sewage treatment system comprising the same | |
| CN106145579B (en) | Alkali residue and excess sludge coupling rotational flow carbon release method and device | |
| CN105366899B (en) | A kind of Fenton oxidation technique of ozone anaerobism iron reduction combination mud decrement | |
| Ye et al. | In-situ ammonia stripping with alkaline fermentation of waste activated sludge to improve short-chain fatty acids production and carbon source availability | |
| CN102452770A (en) | Biochemical treatment/advanced oxidation treatment coupled sewage treatment technique | |
| Yuan et al. | Pilot-scale study of enhanced anaerobic digestion of waste activated sludge by electrochemical and sodium hypochlorite combination pretreatment | |
| CN105417869A (en) | Fenton oxidation-biological combination treatment technology capable of achieving ozone-anaerobic iron reduction and sludge reduction | |
| CN108996865B (en) | Pretreatment method and device for biogas production from sludge | |
| CN104150731B (en) | A kind of method realizing heavy metals in city sewage sludge stabilization that biochemical-physical combines | |
| CN105565620A (en) | Chemical sludge stabilization method and treatment device | |
| CN102775026A (en) | Method for treating biogas slurry by using modified fly ash | |
| Jiang et al. | Microwave-alkali treatment with water elutriation to enhance waste activated sludge solubilization for carbon sources and nutrients recovery | |
| CN108383335B (en) | High-concentration organic wastewater treatment system and method | |
| CN105502842A (en) | Wastewater Fenton oxidation-biological combined treatment method and device capable of recycling sludge | |
| CN105565615A (en) | Technology for carrying out standard treatment on pentaerythritol wastewater | |
| CN101973659A (en) | Device and method for refining waste water by treating vitamin B12 by means of co-use of micro-electrolysis and physicochemical method | |
| CN204958687U (en) | Dyeing and printing auxiliary waste water's processing system | |
| CN104341083A (en) | Pharmaceutical sludge reduction treatment method | |
| CN114804557A (en) | Method for utilizing sludge in-situ micro-channel carbon source | |
| CN104529106B (en) | Copper sulfate promotes the methanogenic method of excess sludge anaerobic digestion | |
| CN105174640A (en) | Biochemical treatment process for paint-producing wastewater | |
| CN113060899B (en) | Recycling method for generating carbon source by utilizing sludge resource of sewage plant | |
| CN109110917A (en) | Magnetic sludge zero-emission sullage continuous processing technique and dedicated unit | |
| CN113003716A (en) | Device and method for synchronously treating nitrite nitrogen wastewater and excess sludge | |
| CN102874987B (en) | Yeast wastewater pretreating method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20220729 |
|
| WW01 | Invention patent application withdrawn after publication |