WO1995026806A1 - Permeation and biological treatment of waste gas - Google Patents
Permeation and biological treatment of waste gas Download PDFInfo
- Publication number
- WO1995026806A1 WO1995026806A1 PCT/GB1995/000744 GB9500744W WO9526806A1 WO 1995026806 A1 WO1995026806 A1 WO 1995026806A1 GB 9500744 W GB9500744 W GB 9500744W WO 9526806 A1 WO9526806 A1 WO 9526806A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- membrane
- dce
- gas
- gaseous stream
- concentration
- Prior art date
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/84—Biological processes
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- VOC's volatile organic compounds
- DCE- dichloroethane chlorinated solvents
- aromatics benzene, toluene
- Biodegradation renders the toxic VOC harmless by converting it into harmless components such as carbon dioxide, water and mineral constituents such as chloride ion.
- a membrane bioreactor can be used to extract toxic VOC's from a waste gas stream, and then biodegrade them.
- the membrane acts as a barrier between the biomedium and the contaminated gas stream (see figure 1) thus avoiding the entry into the biomedium of compounds (such as HC1) , which would hinder biological degradationT
- the solutes may be transferred at a higher rate than in a conventional system since mass transfer through silicone rubber may be faster than mass transfer through a water film.
- microorganisms can be maintained in a favourable growth environment, as they only receive the specific compound they need as carbon source from the gas stream.
- a method of reducing the concentration of at least one gaseous or vapour phase organic compound present in a gaseous stream wherein said gaseous stream is caused to flow in contact with an interior surface of a substantially water-insoluble selectively permeable sheet, tubular or envelope-type polymeric membrane whose permeability to the said at least one organic compound exceeds its permeability to chloride ion, whilst simultaneously maintaining in contact with an external surface of said membrane an aqueous reaction medium containing biologically active reaction means such as biomass bacteria or algae or other microorganisms or immobilised cells capable of reacting with said at least one compound after it permeates from the gaseous stream through said membrane from said interior surface thereof to said external surface.
- biologically active reaction means such as biomass bacteria or algae or other microorganisms or immobilised cells capable of reacting with said at least one compound after it permeates from the gaseous stream through said membrane from said interior surface thereof to said external surface.
- Membrane modules may be constructed in any suitable configuration, e.g. spiral wound flat sheets, layered flat sheets, shell and tube.
- Diagrams showing the operating principle are given in Figure 1, a system configuration including a remote bioreactor and membrane module is given in Figure 3, and operating data from determinations using the system including the remote bioreactor and the membrane module to biodegrade DCE containing waste gas are given in Figure 8.
- a preferred feature of the present invention resides in use of a dense phase, hollow membrane such as a plurality of tubular synthetic elastomers like silicone rubber to create an interface between the gas and aqueous biological phases.
- the present method is particularly useful in gas and vapour permeation, where problems of membrane-fouling or -scaling can be minimised, and parallel reactions may be avoided.
- the selective mass transport allows the recovery of single compounds without an additional process step.
- a membrane process can be described as a special type of extraction process which is more suitable for applications where the organic vapour content is too high to make carbon adsorption feasible, but too low to permit incineration.
- membranes One step further in the use of membranes is the combination of membrane extraction and a subsequent bioconversion.
- Microporous membranes have limited selectivities, which under certain conditions prevent complete VOC extraction. Additionally, the transmembrane pressure difference that destroys the membrane is much lower for microporous membranes, and the pores of the membrane can be blocked by biomass. Therefore, the use of dense membranes to treat VOCs is preferable.
- a strain of microorganisms for example Xanthobacter. autotrophicus GJ10 described by Janssen et al in 1985 is capable of utilising DCE and other haloalkanes that are structurally related to DCE (e.g. 1-chlorobutane, 1-chloropropane, 1, 3-dichloropropane, bromoethane) as sole sources of carbon and energy.
- DCE haloalkanes that are structurally related to DCE (e.g. 1-chlorobutane, 1-chloropropane, 1, 3-dichloropropane, bromoethane) as sole sources of carbon and energy.
- the first step is the conversion of DCE to 2- chloroethanol by a constitutively produced haloalkane dehalogena ⁇ e.
- chloroethanol is converted, via chloroacetaldehyde to 2-chloroacetic acid by a quinoprotein (PQQ) alcohol dehydrogena ⁇ e and a coenzyme (NAD) dependent aldehyde dehydrogenase.
- PQQ quinoprotein
- NAD coenzyme
- the second dehalogenase dechlorinates the 2-chloroacetic acid to glycolic acid which is finally degraded to biomass, water, carbon dioxide and hydrochloric acid.
- the overall stoichiometric equation can be expressed by
- FIG 1 shows the principle of operation of the present membrane bioreactor system
- Figure 2 illustrates mass transfer and biodegradation in a bioscrubber
- FIG. 3 shows a membrane module and remote bioreactor configuration
- FIG. 4 illustrates the metabolic pathway for dichloroethane (DCE) degradation by Xanthobacter autotrophicus GJ10
- Figure 5 shows apparatus for investigating transmembrane transfer of DCE from a waste gas stream into a receiving solution
- Figure 6 shows an apparatus for determination of mass transfer coefficients
- FIG. 7 shows a more detailed arrangement of membrane module and remote bioreactor apparatus for quantitative measurements of DCE extraction and biodegradation
- Figure 8 demonstrates removal efficiency of DCE in the membrane bioreactor
- Figure 9 show the results of transfer test using silicone rubber membrane. DCE concentration curves in the gas vessel are identified thus -A in the receiving solution - ⁇ and in the gas -O
- Figure 10 shows mass transfer results with membrane module (gas flow rate: 750 mL min -1 , receiving solution flow rate: 1050 mL min -1 ) :
- Figure 11 shows mass transfer results with membrane module (gas flow rate: 1500 mL min , receiving solution flow rate: 1050 mL min -1 ) : DCE concentration curves in the gas production vessel (A) , gas inlet (o) , gas outlet (•) and the receiving solution ( ⁇ ),
- Figure 12 shows " mass transfer results with membrane module (gas flow rate: 750 mL min , receiving solution flow rate: 2300 mL min -1 ) : DCE concentration curves in the gas production vessel (A) , gas inlet (o) , gas outlet (•) and the receiving solution ( ⁇ ) ,
- Figure 13 shows mass transfer results with membrane module (gas flow rate: 1500 L min , receiving solution flow rate: 2300 mL min -1 ) : DCE concentration curves in the gas production vessel (A) , gas inlet (o) , gas outlet (•) and the receiving solution ( ⁇ ) ,
- Figure 14 shows the gas flow rate of DCE waste gas
- Figure 15 shows the pressure drop on the shell-side of the membrane
- Figure 16 shows removal efficiency of DCE in the membrane bioreactor
- FIG. 17 shows the flux of DCE through the membrane
- Figure 18 shows carbon evolution: expected values assuming complete mineralisation of DCE to carbon dioxide (A) ; values from the analysis of the gas exhaust of the reactor ( ⁇ ) ; carbon leaving the bioreactor as biomass (o) ,
- Figure 19 shows chloride evolution in the biological medium: expected values assuming complete mineralisation of DCE (A) and measured concentrations ( ⁇ ) .
- the sealed flasks were subsequently analysed for DCE and Cl- concentrations and turbidity. Bacterial growth was observed with increasing turbidity which is proportional to the number of cells in the liquid, and decreasing DCE concentration showing that the microorganisms were able to utilise the provided DCE as a sole carbon source .
- Samples of Xanthobacter autotrophicus GJI O cells were stored in f lasks containing glycerol and placed in a freezer compartment .
- Ta b le 1 Nutrient salts and vitamins medium for Xanthobacter autotrophicus GJ10
- initial column oven temperature 40°C initial time (period in which temperature stays constant): 2 min rate of column over temperature rise: 20C° per min final oven temperature: 100°C final time (period in which temperature is held before the oven is cooled down) 0.5 min
- the concentration of DCE in the sample was calculated as follows:
- the peak area generated by the GC is proportional to the mass of the detected compound.
- the ratio between the amount of DCE and TCE in sample and in the standard can be expressed by
- A is the value for the peak area in %.
- DCE concentration in the waste gas and the exhaust gas was measured in the same GC and using the same temperature program. A 1 mL gas sample was injected into the column and the concentration was calculated against an external liquid standard.
- A is the absolute peak value.
- the factors C-, and C 2 take into account different attenuations and the presence of other compounds in the standard. For the gas measurements, liquid DCE solution was injected and analysed at the same attenuation as the samples, so that these factors became 1.
- Chloride was assayed colorimetrically according to a known technique.
- aqueous sample solution 3.0 L of mercuric thiocyanate solution (1.5 g mercuric thiocyanate in 500 mL of 98% ethanol) and 1.0 mL of iron alumn solution (8g ferric ammonium sulphate in 100 mL 6M nitric acid) were added.
- the mixture was shaken and the colour allowed to develop for 10 min after which the absorption was measured at 460 nm.
- the obtained value was compared with a standard calibration curve and the chloride concentration was calculated by linear interpolation.
- the uncertainty of this assay (quoted as the standard deviation of 5 separate determinations) was 5% at the 10 mg L level.
- Carbon dioxide was measured in an infra-red gas analyser (Servo ex PA 404).
- the principle is based on the fact that many gases and liquids absorb energy in the infra ⁇ red region of the spectrum because of resonant molecular vibrations. These resonances produce highly characterised spectra which can be used to identify substances.
- the gas stream was diverted through a cooler to condense the remaining moisture which might damage the infra-red analyser.
- the analyser read the carbon dioxide concentration in volume percent (volume carbon dioxide per volume air) which was converted in mg L -1 .
- the concentration in the air entering the bioreactor (0.03% - 0.04%) was subtracted.
- an apparatus was constructed corresponding to Figure 5 using a tubular silicone rubber membrane (1 m length, 2 mm inner diameter, 0.5 mm wall thickness), being a commercially available poly(di ethylsiloxane) and inert filler for strength.
- the gaseous waste stream was created by bubbling air into a vessel containing 10L of DCE solution with an initial concentration of 1000 mg L . Due to air stripping, DCE was transferred from the solution to the gaseous phase. This synthetic gas was pumped through the membrane at a flow rate of 0.5 L min . Due to this method used for gas generation, the gas produced also contained water vapour and therefore a humidity trap with silica gel was used to prevent humidity in the gas pump or on the gas side of the membrane. In order to keep constant atmospheric pressure in the gas production vessel, an outlet with an activated carbon trap was installed (see Fig. 5)
- the synthetic DCE gas stream passed through the silicone tubing which was placed in a shakeflask containing the receiving solution.
- This solution was 530 L distilled water at pH 7.0.-
- the shakeflask was kept at a constant temperature of 30°C using a.waterbath.
- All the tubing in the system other than the silicone rubber membrane was of polytetrafluoroethylene (PTFE) which had been chosen to minimise adsorption of DCE from the waste gas and the receiving solution.
- PTFE polytetrafluoroethylene
- the membrane module employed was a spiral wound silicone rubber tubing module with a transfer surface area of 2.5 m .
- the specific surface area a M A H /V M was 1667 m -1 .
- the DCE containing gas was circulated on the tube side at flow rates of 750 and 1500 mL min -1 .
- the gas generation unit used in the previous examples was modified, as the transfer rates were expected to be higher and the concentration in the gas production vessel would consequently decrease rapidly preventing a constant gas flow.
- a high concentration DCE solution (2800-2950 mg L -1 ) was added to the gas production vessel at flow rates that varied between 0.18 and 0.24 mL min -1 , and the same amount of solution was removed from the system via a multichannel peristaltic pump.
- the DCE concentrations in the gas production vessel and in the receiving solution as well as the gas concentrations in the inlet and outlet of the membrane module were measured. Furthermore, the change in concentration of the highly concentrated DCE solution due to volatilisation was monitored.
- the membrane bioreactor system used was similar to the previously described configuration for the determination of mass transfer coefficients.
- the receiving solution vessel was replaced by a continuously stirred tank reactor (CSTR) used as a fermenter.
- CSTR continuously stirred tank reactor
- the CSTR was inoculated with Xanthobacter autotrophicus GJ10 cells grown on DCE under non-sterile conditions.
- the membrane module employed was the same as described above.
- the total biomedium volume was approximately 2 L including volume of the CSTR and membrane hold-up. Gas flow was set at a rate of 100 mL min- entering at the base of the CSTR through a stainless steel sparger. In order to achieve complete mixing and homogeneous aeration, the stirrer speed was set at 500 rpm.
- the temperature of the biomedium was held constantly at 30°C by a temperature controller with a heating element.
- a pH controller held the pH at 7.0 in the biomedium via the adding of acid (IM sulphuric acid solution) or base (IM sodium hydroxide solution) as necessary. Nutrient salt solution was added to the CSTR at a flow rate of 0.95 L min -1 through a multichannel peristaltic pump.
- a water cooled condenser was fitted to the gas outlet to minimise the loss of DCE due to air stripping caused by the aeration of the bioreactor. Gas exiting the reactor was piped either to a fume cupboard or into the sample loop of the C0 2 analyser as required for C0 2 analysis.
- the biomedium was recirculated at an initial flow rate of 2000 L min- on the shell side of the membrane. As the gas flow rate on the tube side, which was initially set at 1500 L min -1 , started to decrease due to membrane expansion, the biomedium flow rate was reduced to 1000 L min . The pressure drop on the biomedium side was measured regularly using a mercury manometer.
- the DCE concentration in the gas entering and exiting the membrane was measured.
- the concentration in the gas production vessel was monitored and the flow rate of the peristaltic pump adding the highly concentrated DCE solution was adjusted to between 0.176 and 0.32 mL min -1 .
- the graphs in Figures 10 to 13 show the results of the mass transfer tests carried out with the membrane module at different flow rates on tube and shell side. The final DCE concentrations at steady state were determined.
- the gas flow rate which was initially set at 1500 mL min -1 , decreased during the operating period due to swelling of the silicone rubber and growth of biomass on the shell- side which caused expansion of the membrane.
- the change of these gas flow rates is shown in Fig. 14.
- the average DCE gas concentration entering the membrane was 0.65 mg L -1 and decreased to a concentration of 0.06 mg L- at the membrane outlet.
- the average removal efficiency shown in Fig. 16 was calculated as the ratio between outlet and inlet concentration and was approximately 91%.
- the flux of DCE across the membrane calculated as the product of the gas flow rate and difference in DCE concentration between membrane inlet and outlet increased within the first two days of running the bioreactor apparatus.
- the concentration in the biomedium increased and subsequently decreased within this time span, as the microorganisms acclimatised to the new growth conditions. After 48 hours, no DCE was detected in the biomedium, and therefore the driving force between gas and liquid phases increased leading to a maximum DCE flux of approximately 55 mg h .
- the amount of carbon exiting the system was measured as C0 2 exiting through the gas outlet of the bioreactor, and as biomass leaving via the biomedium overflow.
- the carbon evolved as C0 2 was calculated as the product of the air flow and the C0 2 concentration measured in the C0 2 analyser.
- the amount of carbon leaving as biomass was obtained from the product of the biomedium flow rate of the overflow and the amount of suspended biomass which stayed constant at a value of 20 mg L -1 .
- the amount of DCE lost due to air stripping was found to be less than 0.8% of the total amount of DCE entering the membrane bioreactor system and could therefore be neglected.
- Fig. 19 shows the measured evolution of chloride ions calculated from the biomedium overflow flow rate and the chloride concentration in the biomedium, and the theoretical evolution of chloride assuming 100% conversion of DCE to chloride.
- a membrane bioreactor system has been used to remove an organic pollutant 1, 2-dichloroethane (DCE) from a gaseous waste stream.
- DCE 2-dichloroethane
- this process allows the treatment of contaminated air streams at low flow rates and with low pollutant concentrations.
- a plurality of elongate, tubular hollow silicone rubber membranes separate the contaminated gas stream from the biomedium. This allows selective transfer of the organic compound through the membrane to the biomedium where biodegradation occurs.
- the conditions in the biomedium can be controlled independently from the waste gas side.
- a gas flow rate of 770 mL min -1 and an average DCE concentration of 0.65 mg L -1 91% of the DCE present in the synthetically produced gaseous stream was biodegraded.
- extensive growth of biofilm attached to the membrane surface on the biomedium side was observed, which caused a pressure drop on the biomedium side of the membrane of approximately 600 bar when steady state conditions were achieved.
- the release of chloride ions due to the mineralisation of DCE was found to be 99%, while conversion of DCE to C0 2 was found to be 60% of the amount of carbon crossing the membrane. This discrepancy is thought to be due to the extensive biofilm formation.
- the mass transfer of DCE across the membrane in absence of microbial activity was also determined. With a gas flow rate of 770 mL min -1 and a water flow rate of 1050 mL min , the overall mass transfer coefficient was determined to be 0.83.10 -3 m s -1 .
- the comparison of the DCE fluxes across the membrane in the presence and absence of microbial activity revealed that the biofilm lowers significantly the amount of DCE crossing the membrane.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP95913276A EP0752909A1 (en) | 1994-03-30 | 1995-03-30 | Permeation and biological treatment of waste gas |
JP7525510A JPH09510917A (en) | 1994-03-30 | 1995-03-30 | Permeation and biological treatment of waste gas |
AU20807/95A AU2080795A (en) | 1994-03-30 | 1995-03-30 | Permeation and biological treatment of waste gas |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB9406323A GB9406323D0 (en) | 1994-03-30 | 1994-03-30 | Treating waste gas |
GB9406323.7 | 1994-03-30 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1995026806A1 true WO1995026806A1 (en) | 1995-10-12 |
Family
ID=10752765
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB1995/000744 WO1995026806A1 (en) | 1994-03-30 | 1995-03-30 | Permeation and biological treatment of waste gas |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP0752909A1 (en) |
JP (1) | JPH09510917A (en) |
AU (1) | AU2080795A (en) |
GB (1) | GB9406323D0 (en) |
WO (1) | WO1995026806A1 (en) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1997019196A1 (en) * | 1995-11-22 | 1997-05-29 | North Carolina State University | Bioreactor process for the continuous removal of organic compounds from a vapor phase process stream |
EP0878214A2 (en) * | 1997-05-15 | 1998-11-18 | Canon Kabushiki Kaisha | Process and apparatus for remedying polluted media |
WO2000000275A1 (en) * | 1998-06-29 | 2000-01-06 | Membrane Extraction Technology Ltd. | Membrane separation involving a two-phase fluid on membrane side |
US8679230B2 (en) | 2008-12-19 | 2014-03-25 | Michael L. Strickland | Reducing emissions of VOCs from low-pressure storage tanks |
EP3026105A1 (en) * | 2014-11-27 | 2016-06-01 | Linde Aktiengesellschaft | Silicone hose for solving CO2 in water for algae production |
CN114558564A (en) * | 2022-01-20 | 2022-05-31 | 北京科技大学 | Charcoal @ metal type denitration catalyst based on active algae and preparation method thereof |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN110339703A (en) * | 2019-07-16 | 2019-10-18 | 成都霸中霸科技发展有限责任公司 | A kind of factory's organic exhaust gas biological cleaning processing unit |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2079460A5 (en) * | 1970-02-02 | 1971-11-12 | Rhone Poulenc Sa | Polyorganosiloxane elastomer membranes - contng zeolite for gaseous separation procedures in conventional appts |
DE3542599A1 (en) * | 1985-12-03 | 1987-06-04 | Ulrich Dipl Ing Baeuerle | Process and apparatus for eliminating sparingly water-soluble and readily volatile impurities from an exhaust air stream or exhaust gas stream by biological oxidation |
DE4027126C1 (en) * | 1990-08-28 | 1991-12-12 | Eberhard Prof. Dr. 2000 Hamburg De Bock | |
US5116506A (en) * | 1989-06-30 | 1992-05-26 | Oregon State University | Support aerated biofilm reactor |
-
1994
- 1994-03-30 GB GB9406323A patent/GB9406323D0/en active Pending
-
1995
- 1995-03-30 WO PCT/GB1995/000744 patent/WO1995026806A1/en not_active Application Discontinuation
- 1995-03-30 EP EP95913276A patent/EP0752909A1/en not_active Withdrawn
- 1995-03-30 AU AU20807/95A patent/AU2080795A/en not_active Abandoned
- 1995-03-30 JP JP7525510A patent/JPH09510917A/en active Pending
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2079460A5 (en) * | 1970-02-02 | 1971-11-12 | Rhone Poulenc Sa | Polyorganosiloxane elastomer membranes - contng zeolite for gaseous separation procedures in conventional appts |
DE3542599A1 (en) * | 1985-12-03 | 1987-06-04 | Ulrich Dipl Ing Baeuerle | Process and apparatus for eliminating sparingly water-soluble and readily volatile impurities from an exhaust air stream or exhaust gas stream by biological oxidation |
US5116506A (en) * | 1989-06-30 | 1992-05-26 | Oregon State University | Support aerated biofilm reactor |
DE4027126C1 (en) * | 1990-08-28 | 1991-12-12 | Eberhard Prof. Dr. 2000 Hamburg De Bock |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1997019196A1 (en) * | 1995-11-22 | 1997-05-29 | North Carolina State University | Bioreactor process for the continuous removal of organic compounds from a vapor phase process stream |
US5954858A (en) * | 1995-11-22 | 1999-09-21 | North Carolina State University | Bioreactor process for the continuous removal of organic compounds from a vapor phase process stream |
EP0878214A2 (en) * | 1997-05-15 | 1998-11-18 | Canon Kabushiki Kaisha | Process and apparatus for remedying polluted media |
EP0878214A3 (en) * | 1997-05-15 | 2000-04-05 | Canon Kabushiki Kaisha | Process and apparatus for remedying polluted media |
US6319706B1 (en) | 1997-05-15 | 2001-11-20 | Canon Kabushiki Kaisha | Process and apparatus for remedying polluted media |
WO2000000275A1 (en) * | 1998-06-29 | 2000-01-06 | Membrane Extraction Technology Ltd. | Membrane separation involving a two-phase fluid on membrane side |
US8679230B2 (en) | 2008-12-19 | 2014-03-25 | Michael L. Strickland | Reducing emissions of VOCs from low-pressure storage tanks |
EP3026105A1 (en) * | 2014-11-27 | 2016-06-01 | Linde Aktiengesellschaft | Silicone hose for solving CO2 in water for algae production |
CN114558564A (en) * | 2022-01-20 | 2022-05-31 | 北京科技大学 | Charcoal @ metal type denitration catalyst based on active algae and preparation method thereof |
CN114558564B (en) * | 2022-01-20 | 2022-12-30 | 北京科技大学 | Charcoal @ metal type denitration catalyst based on active algae and preparation method thereof |
Also Published As
Publication number | Publication date |
---|---|
EP0752909A1 (en) | 1997-01-15 |
AU2080795A (en) | 1995-10-23 |
GB9406323D0 (en) | 1994-05-25 |
JPH09510917A (en) | 1997-11-04 |
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