CN101250004A - Device and method for improving function of CH4 production by UASB and removal rate of phosphate by using zero-valent iron - Google Patents
Device and method for improving function of CH4 production by UASB and removal rate of phosphate by using zero-valent iron Download PDFInfo
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- CN101250004A CN101250004A CNA2008100103816A CN200810010381A CN101250004A CN 101250004 A CN101250004 A CN 101250004A CN A2008100103816 A CNA2008100103816 A CN A2008100103816A CN 200810010381 A CN200810010381 A CN 200810010381A CN 101250004 A CN101250004 A CN 101250004A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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Abstract
The invention relates to the technical field of biological treatment of waste water, in particular to a device and a method for increasing CH4 function produced by UASB with zero valent iron and phosphate removal rate. The device is a UASB reactor and a hydraulic circulating pathway, which comprises a granular sludge bed, a three-phase separator and a hydraulic circulating device. The reactor main body, the granular sludge bed and the hydraulic circulating device are connected and form a ring-shaped conduit line, a water inlet distribution device is arranged on the conduit line among the hydraulic circulating device, the reactor main body and the granular sludge bed, and a zero valent iron container for containing zero valent iron 7 is disposed between the water inlet distribution device 1 and the hydraulic circulating device 2. The method includes that the amount of zero valent iron added to the zero valent iron container is 10-100g/l, and the reactor operates stably at a temperature from 25 DEG C to 35 DEG C or from 45 DEG C to 55 DEG C. For an improvised UASB reactor, the COD removal rate is increased 6.5% in average, the methane production capacity is improved 10.2%, and the phosphate removal rate of the UASB reactor is close to 80%.
Description
Technical field
The present invention relates to the biological wastewater treatment technology field, specifically a kind of with Zero-valent Iron raising UASB product CH
4The apparatus and method of effect and phosphoric acid salt clearance.
Background technology
Along with the continuous quickening and the expanding economy of process of industrialization, a large amount of undressed or handle below standard worker, agricultural effluent is discharged in the receiving water body, has caused extensive and serious water pollution problems.Compare with physics, chemical treatment method with traditional aerobic biological process for treating, the Anaerobic Microbiological Treatment Technology of waste water has the volumetric loading height, device structure is simple, running maintenance is convenient, floor space is little, energy consumption is low, excess sludge is few, produce renewable energy source (CH
4) etc. advantage.This technology is to remove the effective way of organic pollutant in the water body, obtains application more and more widely at home and abroad during industry and sanitary wastewater are handled at present.In addition, Anaerobic Microbiological Treatment Technology also is considered to meet one of " continuable development principle " core technology.
Anaerobic biological treatment technology is referred to as anaerobic digestion traditionally, and (anaerobic digestion AD), also claims sludge digestion (sludge digestion).The essence of anaerobic biological treatment is meant that the complicated organism (carbohydrate, protein, lipid etc.) that contains in the waste water under anaerobic passes through the cometabolism of multiple microorganism, finally is converted into CH
4, CO
2Deng.Organic anaerobic biological treatment is divided into two stages: hydrolysis stage; The acidogenic fermentation stage; Produce hydrogen and produce the acetate stage; Produce methane phase.Produce acid and produce methane phase.Hydrolysis can be defined as under the effect of organic substance lytic enzyme outside the acid formers born of the same parents of complicated non-solubility and be converted into simple solvability monomer or dimeric process.In anaerobic digestion process, organism that number molecular weight is bigger such as starch are decomposed into maltose and glucose by amylase, and protein is become small peptide and amino acid etc. by protease hydrolysis.Organism with hydrolysate-solvability monomer or dimeric forms is converted into based on lipid acid and pure end products microorganism (acidogenic fermentation bacterium) in this stage, produces new cellular material simultaneously.Acidogenic fermentation speed is very fast, and end products mainly contains lipid acid such as formic acid, acetate, propionic acid, butyric acid, valeric acid, caproic acid, lactic acid.In addition, alcohols, CO
2, H
2Deng also supervening.Producing hydrogen product acetate process is that two organic acid (except the acetate) and alcohol more than the carbon that the acidogenic fermentation stage produces are converted into acetate, CO
2, H
2Deng process, and produce new cellular material.Produce methane phase and be methanogen by strictly anaerobic with acetate, formic acid, methyl alcohol, methylamine and H
2/ CO
2Deng being converted into CH
4And CO
2Process.
Up-flow anaerobic sludge blanket treatment technology (UASB) is typical case's representative of anaerobic waste water biologic treating technique.Since twentieth century UASB seventies technology is invented, obtained tremendous development by updating, the UASB technology has become one of mainstream technology of domestic and international anaerobic treatment in recent years.At present having had the UASB reactor of more than 1300 through engineering approaches to be successfully applied in various concentration, the polytype biological wastewater treatment process all over the world, is the anaerobic biological reactor that is most widely used.
The main treating processes of UASB technology is as follows: pending waste water is introduced into the bottom of UASB reactor, the Sludge Bed of upwards flowing through and forming by particulate state or floc sludge, sewage contacts with Sludge Bed and anaerobic reaction takes place and produce biogas (being mainly methane and carbonic acid gas), the biogas that produces rise and cause the Sludge Bed disturbance and drive granule sludge and rise, under the effect of triphase separator, granule sludge is descended, get back to the Sludge Bed zone, thereby form the internal recycling of granule sludge, the biogas that produces utilize through being collected behind the triphase separator again, sewage is discharged system after treatment.In general, the UASB reactor need keep a stable up-flow speed by a waterpower circulation device, thereby is formed and keep the good granule sludge of sedimentation function, and this is a key normally moving the UASB system.The general main following a few part that comprises of UASB system: water inlet and water dispensing apparatus 1, waterpower circulation device 2, reactor body 3 and three separators 4 (referring to 1).
Iron is one of metallic element that content is the abundantest and activity is very strong in the earth's crust.Iron and ionic compound thereof have been widely used in water body reparation and field of waste water treatment as flocculation agent, redox reaction catalyzer.In the last few years, organochlorine contamination thing, heavy metal or even the nuke rubbish pollutent used in zeroth order iron railings or the other forms of elemental iron removal underground water have caused the extensive concern of scientific circles, though organic pollutant wherein is adsorbed, concrete mechanism fixing and degraded is not also known by the people.In addition, Zero-valent Iron (Fe
0) can be used as electron donor, utilized in pollutent reduction conversion process by many microorganisms.Therefore, Fe
0-microflora manifests increasing potentiality in the biological restoration field of polluting.
The pure culture of methanogen also can utilize Fe
0As unique electron donor with CO
2Be reduced to CH
4Under anaerobic, work as Fe
0When being immersed in the water, Fe
0Can lose 2e, form Fe
2+, the H in the water
+Obtain forming negative electrode H behind the electronics
2, and H
2Can by methanogen or other can metabolism hydrogen microorganism constantly utilize and consume Fe
0Betatopic process will constantly be carried out.In other words, Fe
0Oxidising process join with production by biological methane process phase coupling.These bite the hydrogen microorganism can remove the metallic surface in the process of ferroelectric chemical oxidation hydrogen protective layer, have brought into play unpolarizing, make Fe
0Oxidation continues to take place.
The UASB technology still has some limitation in its further wide popularization and application at present, as: lower in temperature, organic loading is lower or waste water under the more situation of difficult degradation composition, its processing efficiency is undesirable, in addition, the scarce capacity of nutritive elements such as the nitrogen in the UASB reactor removal waste water, phosphorus.In recent years, various countries scientist and technician conduct a research respectively from different perspectives, remove efficient with COD removal ability, product methane ability and the nitrogen phosphorus of further raising up-flow anaerobic sludge blanket.
Summary of the invention
The object of the invention is to provide a kind of and improves the apparatus and method that UASB produces CH4 effect and phosphoric acid salt clearance with Zero-valent Iron.
For achieving the above object, the technical solution adopted in the present invention is:
Device: UASB reactor waterpower circulating path comprises reactor body and granular mud bed, triphase separator and waterpower circulation device, triphase separator, reactor body and granular mud bed and waterpower circulation device connect into circular line, waterpower circulation device and reactor body and granular mud bed between pipeline be provided with into water and water dispensing apparatus, the water inlet and water dispensing apparatus 1 and waterpower circulation device 2 between be provided with the Zero-valent Iron container 7 that takes up Zero-valent Iron.The inlet of described Zero-valent Iron container 7 links to each other with the water outlet of waterpower circulation device 2, and outlet converges mutually with the water outlet of water inlet and water dispensing apparatus 1, is connected with the import of reactor body and granular mud bed 3.
Method: adding the Zero-valent Iron amount in the Zero-valent Iron container is 10-100g/l; The operation temperature of UASB reactor is 25-35 ℃ or 45-55 ℃ of steady running.The Zero-valent Iron of described interpolation is an iron powder, can be micron order iron powder or nano grade iron powder, micron order iron powder purity＞99% wherein, and particle diameter is 0.02～0.10mm, specific surface area is 0.7～1.0m
2/ g; Nano grade iron powder purity＞99%, particle diameter are 30～100nm, and specific surface area is 70～150m
2/ g.The organic loading of UASB reactor operation is at 0.120.0kg/m
3.d.
The advantage that the present invention had:
The present invention adds a supplementary unit-Zero-valent Iron container in the waterpower circulating path of existing UASB reactor, place iron powder in the container.It passes through under anaerobic, and Zero-valent Iron makes the sewage treating efficiency of UASB reactor obtain to improve to the multiple special reinfocing effect of anerobic sowage processing.The method of interpolation Zero-valent Iron is improved up-flow anaerobic sludge blanket technology and is reached the raising reactor and produces the methane ability, improves COD removal ability and phosphoric acid salt removal ability.The result shows: the UASB reactor after the improvement can make handles COD efficient raising 6.5%, produce the methane ability and improve 10.2%, and the phosphatic removal efficient of UASB reactor is near 80%.This improvement is very little to the device structure and the operational conditions influence of original system, and the cost increase is also very little.
Description of drawings
Fig. 1 is conventional UASB reactor assembly synoptic diagram.
Fig. 2 is a UASB reactor assembly synoptic diagram of the present invention.
Main label is 1. water inlet and water dispensing apparatus, 2. waterpower circulation device, 3. reactor body and granular mud bed, 4. triphase separator, 5. sludge gas collecting device, 6. water outlet, 7. Zero-valent Iron containers.
Embodiment
Improve UASB reactor methanogenesis and phosphoric acid salt and remove the device of efficient.Pipeline between conventional UASB reactor waterpower circulation device 2 and reactor body and granular mud bed 3 is provided with into water and water dispensing apparatus 1, is provided with the Zero-valent Iron container 7 that takes up Zero-valent Iron between water inlet and water dispensing apparatus 1 and the waterpower circulation device 2.The inlet of described Zero-valent Iron container 7 links to each other by pipeline with the water outlet of waterpower circulation device 2, and outlet converges with the water outlet pipeline of water dispensing apparatus 1 mutually with water inlet, be connected with the pipeline of the import of reactor body and granular mud bed 3.
Method: in the operational process of UASB system, waste water is handled the rear section water outlet through UASB and is entered Zero-valent Iron container 7 through waterpower circulation device 2, mainly contains two processes in the Zero-valent Iron container: the one, and some difficult degradations in the waste water organise and thing and the effect of active metal Zero-valent Iron have further improved biodegradability; The 2nd, the part zeroth order iron powder in the container is along with recirculated water enters in the UASB reactor granules Sludge Bed 3.Under anaerobic, following electrochemical reaction can take place in Zero-valent Iron:
Anodic reaction: Fe-2e → Fe
2+E
0(Fe
2+/ Fe)=-0.440V;
Cathodic reaction: 2H
++ 2e → 2[H] → H
2↑ ... E
0(H
+/ H
2)=0.00V; The H that negative electrode produces
2Can be by the reduction of the methanogen utilization in anaerobic sludge CO
2Generate CH
4Along with H
2Constantly utilized, above-mentioned reaction continues to carry out.[H] also is a kind of strong reductant, the further deoxidization, degradation of the organic compound in the waste water can be improved its biodegradability, is beneficial to organic pollutant and is degraded by microorganisms in the UASB reactor.The Fe that produces
2+Can with water in [OH
-] formation Fe (OH)
2, this compound is a kind of flocculation agent, can further remove the suspended substance in the waste water, has strengthened the settlement action of anaerobic sludge simultaneously, is of value to realizing good mud-water separation process in the UASB reactor.
Embodiment 1
Be processed into a laboratory scale UASB reactor of cover and conventional each cover of UASB reactor according to the method for the invention.Except the Zero-valent Iron container, all parameters of two cover UASB reactors are all identical.The useful volume of reactor is 2.3L, and the Zero-valent Iron container volume is 0.5L, the zeroth order iron powder amount 50g of dispensing wherein, and the physical properties of iron powder is: the micron order iron powder, purity＞99%, particle diameter are 0.05mm, specific surface area is 0.9m
2/ g.The UASB reactor is process object with the wastewater from vitamin C production, and 30 ℃ of steady runnings more than 200 day, reactor can be divided into three phases in handling the waste water process behind the reactor inoculation anaerobic digester mud, and its organic loading is respectively 1.0,5.6 and 10.8kg/m
3.d.Its treatment effect is as shown in table 1.
| Table 1.Fe 0Remove the influence of efficient to improving UASB methanogenesis and phosphoric acid salt | ||||||
| UASB reactor operating parameter | Subordinate phase (n=35) | Phase III (n=23) | Quadravalence section (n=47) | |||
| R 0 | R Fe | R 0 | R Fe | R 0 | R Fe | |
| Biogas yield (m 3/mr 3·d) CH 4Content (%) COD clearance (%) phosphoric acid salt clearance (%) SMA ＊＊ (gCH 4-COD/gVSS·d) | 0.5 a(0.4) 69.1 a(1.8) 65.1 a(18.1) 18.0 A(12.4) 1.12 a(0.40) | 0.6 b(04) 76.5 b(3.0) 78.3 b(19.2) 78.5 B(24.5) 1.17 b(0.36) | 4.5 a(1.3) 69.6 A(2.7) 87.5 A(3.9) 16.1 A(10.3) 1.83 a(0.35) | 5.3 b(1.5) 77.6 B(4.1) 92.9 B(4.5) 78.2 B(21.0) 1.96 b(0.42) | 6.3 A(0.4) 70.8 A(2.1) 89.2 A(2.6) 14.4 A(8.4) 2.45 a(0.21) | 6.7 A(0.4) 79.6 B(2.7) 95.3 A(2.2) 80.3 B(17.0) 2.57 b(0.10) |
| ＊Measure number of times; ＊＊SMA at second and third, the quadravalence section measures respectively 3,2 and 3 times; Numerical value is standard deviation in the bracket; a，bSignificant difference (P＜0.05) A，BDifference is (P＜0.01) extremely significantly; R 0Be control reactor, R FeFor adding the UASB reactor of Zero-valent Iron; SMA is the mud methanogenesis activity | ||||||
As shown in table 1, after wastewater from vitamin C production is handled through UASB, add the UASB reactor (R of Zero-valent Iron
Fe) treatment effect obviously be better than not adding the control reactor (R of Zero-valent Iron
0) handle: fs, R
FeCOD clearance, phosphoric acid salt clearance, biogas in methane content be respectively 78.3%, 78.5% and 76.5%, be significantly higher than R
065.1%, 18.0% and 69.1%.R
FeBiogas yield and the mud methanogenesis activity also than R
0High.Subordinate phase, the organic loading of reactor is at 5.6kg/m
3.d, R
FeCOD clearance, phosphoric acid salt clearance, biogas in methane content be respectively 92.9%, 78.2% and 77.6%, be significantly higher than R
087.5%, 16.1% and 69.6%.The effect of phase III is similar to first and second stage.This shows that adding for improving UASB reactor methanogenesis and phosphatic clearance effect of Zero-valent Iron is remarkable.
Embodiment 2
Above-mentioned laboratory scale UASB reactor is used for the processing of sanitary sewage.The zeroth order iron powder amount 80g of dispensing in the Zero-valent Iron container wherein, the physical properties of iron powder is: nano grade iron powder, its purity＞99%, particle diameter are 40nm, specific surface area is 140m
2/ g.The UASB reactor is process object with the sanitary sewage, and 55 ℃ of steady runnings more than 100 day, the organic loading of reactor stationary phase in handling the waste water process was 1.2kg/m behind the reactor inoculation anaerobic digester mud
3.d.Concrete treatment effect is as shown in table 2.
| Table 2. is added the UASB reactor for treatment sanitary wastewater effect of Zero-valent Iron | ||
| R 0 | R Fe | |
| Biogas yield (m 3/mr 3·d) | 0.18 | 0.22 |
| CH 4Content (%) | 67.5 | 72.5 |
| COD clearance (%) | 62.1 | 80.3 |
| Phosphoric acid salt clearance (%) | 13.0 | 81.5 |
As can be seen from Table 2, when handling sanitary wastewater, adopt UASB reactor R of the present invention
FeCOD clearance, phosphoric acid salt clearance, biogas in methane content be respectively 80.3%, 81.5% and 72.5%, be significantly higher than R
062.1%, 13.0% and 67.5%.R
FeBiogas yield is 0.22m
3/ mr
3.d, be higher than the biogas yield 0.18m that contrasts R0
3/ mr
3.d.
Embodiment 3
Difference from Example 1 is:
The zeroth order iron powder amount 30g of dispensing in the described Zero-valent Iron container, the operation temperature of UASB reactor is 25-35 ℃ of steady running.The Zero-valent Iron of described interpolation is an iron powder, is specially the micron order iron powder, and its purity＞99%, particle diameter are 0.02mm, and specific surface area is 0.8m
2/ g.The organic loading of UASB reactor operation is at 20.0kg/m
3.d.
Embodiment 4
Difference from Example 1 is:
The zeroth order iron powder amount 10g of dispensing in the described Zero-valent Iron container, the operation temperature of UASB reactor is 45-55 ℃ of steady running.The Zero-valent Iron of described interpolation is an iron powder, is specially nano grade iron powder, and its purity＞99%, particle diameter are 100nm, and specific surface area is 70m
2/ g.The organic loading of UASB reactor operation is at 15kg/m
3.d.
Embodiment 5
Difference from Example 1 is:
The zeroth order iron powder amount 60g of dispensing in the described Zero-valent Iron container, the Zero-valent Iron of described interpolation is an iron powder, is specially the micron order iron powder, and its purity＞99%, particle diameter are 0.05mm, and specific surface area is 0.9m
2/ g.The organic loading of UASB reactor operation is at 0.5kg/m
3.d.
Embodiment 6
Difference from Example 1 is:
The zeroth order iron powder amount 90g of dispensing in the described Zero-valent Iron container, the Zero-valent Iron of described interpolation is an iron powder, is specially nano grade iron powder, and its purity＞99%, particle diameter are 50nm, and specific surface area is 90m
2/ g.The organic loading of UASB reactor operation is at 2kg/m
3.d.
Embodiment 7
Difference from Example 1 is:
The zeroth order iron powder amount 20g of dispensing in the described Zero-valent Iron container, the Zero-valent Iron of described interpolation is an iron powder, is specially nano grade iron powder, and its purity＞99%, particle diameter are 90nm, and specific surface area is 120m
2/ g.The organic loading of UASB reactor operation is at 8kg/m
3.d.
Claims (5)
1. one kind is improved UASB with Zero-valent Iron and produces CH
4The device of effect and phosphoric acid salt clearance, UASB reactor waterpower circulating path comprises reactor body and granular mud bed, triphase separator and waterpower circulation device, triphase separator, reactor body and granular mud bed and waterpower circulation device connect into circular line, waterpower circulation device and reactor body and granular mud bed between pipeline be provided with into water and water dispensing apparatus, it is characterized in that: the water inlet and water dispensing apparatus (1) and waterpower circulation device (2) between be provided with the Zero-valent Iron container (7) that takes up Zero-valent Iron.
2. improve UASB product CH by claim 1 is described with Zero-valent Iron
4The device of effect and phosphoric acid salt clearance, it is characterized in that: the inlet of described Zero-valent Iron container (7) links to each other with the water outlet of waterpower circulation device (2), and outlet converges mutually, is connected with the import of reactor body and granular mud bed (3) with the water outlet of water inlet and water dispensing apparatus (1).
3. one kind is improved UASB with Zero-valent Iron and produces CH by claim 1 is described
4The method of effect and phosphoric acid salt clearance is characterized in that: adding the Zero-valent Iron amount in the Zero-valent Iron container is 10-100g/l; The operation temperature of UASB reactor is 25-35 ℃ or 45-55 ℃ of steady running.
4. improve UASB product CH by claim 1 is described with Zero-valent Iron
4The effect and the method for phosphoric acid salt clearance, it is characterized in that: the Zero-valent Iron of described interpolation is an iron powder, can be micron order iron powder or nano grade iron powder, micron order iron powder purity＞99% wherein, particle diameter is 0.02～0.10mm, specific surface area is 0.7～1.0m
2/ g; Nano grade iron powder purity＞99%, particle diameter are 30～100nm, and specific surface area is 70～150m
2/ g.
5. improve UASB product CH by claim 1 is described with Zero-valent Iron
4The method of effect and phosphoric acid salt clearance is characterized in that: the organic loading of UASB reactor operation is at 0.1-20.0kg/m
3.d.
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|---|---|---|---|
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100103816A CN101250004A (en) | 2008-02-05 | 2008-02-05 | Device and method for improving function of CH4 production by UASB and removal rate of phosphate by using zero-valent iron |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060368A (en) * | 2010-11-24 | 2011-05-18 | 南京大学 | Method for improving utilization rate of zero-valent iron in zero-valent iron pretreatment of chemical wastewater |
| CN102140001A (en) * | 2010-12-17 | 2011-08-03 | 合肥工业大学 | Method for increasing methane production efficiency in organic waste anaerobic process |
| CN102976488A (en) * | 2012-11-20 | 2013-03-20 | 浙江大学 | Method for zero-valent nano-iron-reinforced biological removal of nitrogen and phosphorus |
| CN104045151A (en) * | 2014-06-26 | 2014-09-17 | 清华大学 | In-situ methane purifying reactor based on bioelectrochemical principle and in-situ methane purifying method |
| CN105236565A (en) * | 2015-07-02 | 2016-01-13 | 中国环境科学研究院 | Magnetic-field-strengthening method for increasing COD (Chemical Oxygen Demand) removal efficiency of anaerobic wastewater treatment by iron powder |
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| CN106746010A (en) * | 2016-12-30 | 2017-05-31 | 四川师范大学 | The processing method of chromate waste water |
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| CN109209268A (en) * | 2018-10-19 | 2019-01-15 | 中国石油集团渤海钻探工程有限公司 | The method that drain is returned in acidification is handled using reproducibility iron powder |
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|---|---|---|---|---|
| CN102060368A (en) * | 2010-11-24 | 2011-05-18 | 南京大学 | Method for improving utilization rate of zero-valent iron in zero-valent iron pretreatment of chemical wastewater |
| CN102140001A (en) * | 2010-12-17 | 2011-08-03 | 合肥工业大学 | Method for increasing methane production efficiency in organic waste anaerobic process |
| CN102976488A (en) * | 2012-11-20 | 2013-03-20 | 浙江大学 | Method for zero-valent nano-iron-reinforced biological removal of nitrogen and phosphorus |
| CN102976488B (en) * | 2012-11-20 | 2013-11-20 | 浙江大学 | Method for zero-valent nano-iron-reinforced biological removal of nitrogen and phosphorus |
| CN104045151A (en) * | 2014-06-26 | 2014-09-17 | 清华大学 | In-situ methane purifying reactor based on bioelectrochemical principle and in-situ methane purifying method |
| CN104045151B (en) * | 2014-06-26 | 2015-09-30 | 清华大学 | A kind of in-situ biogas purified reaction device based on bioelectrochemistry principle and method |
| CN105502870B (en) * | 2014-09-25 | 2019-01-29 | 锐博环保科技(北京)有限公司 | A kind of Zero-valent Iron reinforcement sludge anaerobism pre-reaction device and sludge pre-treatment method |
| CN105502870A (en) * | 2014-09-25 | 2016-04-20 | 锐博环保科技(北京)有限公司 | Zero-valent iron strengthened sludge anaerobic pre-reaction device and sludge pretreatment method |
| CN105236565A (en) * | 2015-07-02 | 2016-01-13 | 中国环境科学研究院 | Magnetic-field-strengthening method for increasing COD (Chemical Oxygen Demand) removal efficiency of anaerobic wastewater treatment by iron powder |
| CN105236565B (en) * | 2015-07-02 | 2017-12-12 | 中国环境科学研究院 | A kind of method that magnetic field-intensification iron powder improves Anaerobic wastewater treatment COD removal efficiency |
| CN106755139A (en) * | 2016-11-29 | 2017-05-31 | 湖南大学 | The method that anaerobic grain sludge efficiently produces propionic acid and valeric acid is cultivated under a kind of sour environment |
| CN106755139B (en) * | 2016-11-29 | 2021-07-30 | 湖南大学 | Method for efficiently producing propionic acid and valeric acid by culturing anaerobic granular sludge in acidic environment |
| CN106746010A (en) * | 2016-12-30 | 2017-05-31 | 四川师范大学 | The processing method of chromate waste water |
| CN109209268A (en) * | 2018-10-19 | 2019-01-15 | 中国石油集团渤海钻探工程有限公司 | The method that drain is returned in acidification is handled using reproducibility iron powder |
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