|Publication number||US4297216 A|
|Application number||US 05/867,361|
|Publication date||Oct 27, 1981|
|Filing date||Jan 5, 1978|
|Priority date||Jan 22, 1975|
|Also published as||DE2602325A1, DE2602325B2|
|Publication number||05867361, 867361, US 4297216 A, US 4297216A, US-A-4297216, US4297216 A, US4297216A|
|Inventors||Masahiko Ishida, Ryooichi Haga, Youji Odawara|
|Original Assignee||Hitachi, Ltd.|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (8), Referenced by (49), Classifications (16)|
|External Links: USPTO, USPTO Assignment, Espacenet|
This is a continuation of application Ser. No. 651,586 filed Jan. 1, 1976, now abandoned.
This invention relates to a method and a system for treatment of biochemical waste, and more particularly to an improvement of a method of anaerobic treatment of the biochemical waste.
Recently, in accordance with the spread of secondary treating facilities for sewage and waste-water sludge from stock breeding industry, a large amount of surplus activated sewage is continuously produced. In addition, garbage from the human life accumulates to a large amount.
The biochemical waste is mainly formed of the activated sewage and the garbage. Raw sewage contains organic material formed of fats, proteins, carbohydrates and microorganisms. Accordingly, it is very important to efficiently treat the biochemical waste which essentially consists of animal and plant cells and microorganisms.
The anaerobic digestion process has been popular in the waste treatment. It is characterized by the capability of treating large volumes of dilute organic slurries at low cost, because the produced gas can be used for motive power of treating facilities, the high kill rate of pathogenic organisms and the capability of producing solid residues suitable for use as soil conditioners.
Despite its many advantages, the anaerobic digestion process has not yet reached its full potential, because the anaerobic digestion process normally requires long terms such as 40 days for a low treatment efficiency. Therefore nowadays the anaerobic digestion process is not used vigorously.
If the rise of the treatment efficiency can be attained, the anaerobic digestion process is very useful for its many advantages. Various high speed digestion processes which can treat the biochemical waste in fourteen or fifteen days have been provided. But those processes unavoidably sacrifice their digestion rates. This means that those processes have advantages referring to a volume decrease of waste and a rise of dehydration, but they do not satisfy the requirements referring to the useful utilization of digestion gas and the level of BOD (biochemical oxygen demand) of the separated liquid.
The surplus activated sewage is treated by the anaerobic digestion process at a temperature of from 20° to 50 C. for long periods of time while the sewage is concentrated to about from 1 to 570 solids by a settling basin or a centrifuge. During the stay, sewage bacteria are gradually liquefied by the action of anaerobic bacteria to convert to methane gas through organic acid. The methane-producing bacteria are among strictly anaerobic organisms known.
It is well know among those people in this art that if during the stay the sewage in a state of slurry is not well stirred, the digestion remarkably delays and the removing rate of BOD becomes low.
General biochemical waste including surplus activated sewage is a kind of hydrophilic colloid and in a state of almost hydrated gel. Therefore, the sewage of solid density of 5% presents a state of paste and needs a large stirring power. Accordingly, actually the sewage of solid density up to about 5% only have been treated.
The need for improving anaerobic digestion technology is therefore greater now than ever before.
An object of the present invention is to provide an improved method for treatment of biochemical waste which have a high treatment efficiency and a high digestion rate.
Another object of the present invention is to provide an anaerobic process which enables to treat biochemical waste with a high solid density.
A further object of the present invention is to provide an economical anaerobic process which can make stirring power small.
The present invention provides a method for treatment of biochemical waste, comprising the steps of adding acid to the biochemical waste to adjust pH thereof below 3.5, heating the adjusted biochemical waste in a range of temperature between 60° and 200° C. for a predetermined time, adding alkali thereto to neutralize the wate, and treating with anaerobic digestion in a range of from the above mentioned temperature to a normal temperature. Upon the neutralization, it is not necessary to adjust pH to just 7. It is sufficient, if pH is in a range between 5 and 8.
These and other objects of the invention, as well as many of the attendant advantages thereof, will become more readily apparent when reference is made to the following description taken in conjunction with the accompanying drawing, in which:
FIG. 1 is a schematic plan view of the invention, showing a biochemical waste treatment plant embodying the present invention;
FIG. 2 is a set of curves comparing a digestion effect of a prior art and a digestion effect operated in accordance with the invention, when the invention is applied to surplus activated sewage.
In general in anaerobic digestion, organisms and animal and plant cell in raw slurry are liquefied by action of anaerobic bacteria and then converted to organic acid, which is converted to methane by action of methane-producing bacteria.
The anaerobic digestion gradually proceeds through the stay of from 20 to 40 days within a digestion tank. This invention is characterized in that the liquefying process consists of a heat treatment of biochemical waste under acidity. The heat treatment under acidity makes a digestion term short, gas production speed fast and an amount of gas production high. Furthermore, viscosity of biochemical waste remarkably becomes small by employing the heat treatment under acidity, so that the stirring power of a digestion tank is reduced or even biochemical waste of high density above 5% can be thrown out into the system. A pretreatment according to the invention consists of adding acid to the biochemical waste to adjust an effective range of pH below 3.5. Lower values of pH are desirable, but economically the range of pH preferably is between 1.0 and 3.0. Sulfuric acid and hydrochloric acid can be employed for acidifying the biochemical waste and organic acid such as acetic acid and citric acid also is useful. Economically sulfuric acid and hydrochloric acid are suitable and acid of high density is convenient for small dilution. An adding amount of acid is different in accordance with kinds of raw wastes, density and kinds of acids.
In general for forming the above mentioned effective range of pH, when hydrochloric acid of 35% is employed, an amount of the hydrochloric acid ranges between 0.1 and 1% (wt/wt).
When the biochemical waste is in a state of neutrality, there is very little decrease in viscosity as the temperature is raised until the temperature is raised over 150° C. When the biochemical waste is in a state of alkalinity, it would have an even greater viscosity and therefore be undsatisfactory.
It is necessary to continue to heat the biochemical waste over 60° C. and below 200° C. during at least one minute.
A treatment at conditions of excessive high temperatures and long terms, for example at 170° C. and during 20 minutes is not desirable because decomposed products which cause prevention of digestion appear at said conditions.
Thus the heat treatment preferably is at conditions under 160° C. and less than 10 minutes.
FIG. 1 is a block diagram of the flow of biochemical waste through a system including the digester of the present invention. The raw waste can be collected in a settling tank 10 and transferred from the settling tank 10 to a pretreatment tank 13 provided with a heater 14 through a conduit 12 by techniques conventional in the art. Acid is added into the pretreatment tank 13 through a conduit 16 from an acid storage tank 15 to adjust pH of the water. The stirring is continued during heating for promoting its liquefaction.
The pretreated waste is transferred to a digestion tank 20 through a conduit 19. Alkali is added into the digestion tank 20 through a conduit 18 from an alkali storage tank 17 to neutralize the waste. After the neutralization, anaerobic sludge is added into the digestion tank as a seed for anaerobic digestion through a conduit 22 from an anaerobic sludge tank 21.
Anaerobic digestion is continued in the anaerobic environment, whereby digestion gas is produced and taken out through a conduit 23. The remainder is introduced into a digestion sludge separator 24 through a conduit 26. The remainder is separated in the separator 24 into liquid and digestion sludge. The separated liquid is taken out from a conduit 28 and the digestion sludge is taken out from a conduit 29. One part of the digestion sludge is returned into the anaerobic digestion sludge tank 21 through a conduit 30, so that the recycling of the digestion sludge is formed.
The waste from the pretreatment tank 14 may be introduced into a liquefying tank 32 through a conduit 34 shown by a dotted line instead of directly into tank 20. Alkali from a storage tank 36 may be added into the liquefying tank 32 through a conduit 37 to adjust pH of the waste. After the liquefying the waste is returned to the conduit 19 through a conduit 38 shown by dotted line. With such a variation, tank 17 and conduit 18 would be eliminated.
Hydrochloric acid of 2.4 ml, of which density was 35%, was added to surplus activated sludge of 500 g which was remainder of an urban sewage treatment. The solid density of the sludge was 1.5% (wt/wt) and the content of organic material was 62% (wt/wt). The sludge was stirred. Thus, the pH of the sludge was adjusted to 2.0. The sludge was introduced into a stainless beaker and heated at 95° C. for five minutes. After heating, sodium hydroxide of 5 g, of which density was 30%, was added to the sludge so that pH of the sludge was adjusted to 6.9. The adjusted sludge was introduced into a digestion tank and anaerobic digestion sludge of 2 g consisting of excrement was added into the tank as a seed sludge. Gas within a chamber of the tank was replaced by N2 gas. While the adjusted sludge was stirred between 150 and 200 rpm, the anaerobic digestion was continued at 20° C. FIG. 2 shows the result of the anaerobic digestion treatment. In comparison with the result, a result of another identical anaerobic digestion treatment without the pretreatment of the adding acid, the heating and the neutralizing is also shown in FIG. 2. A and B show the processes with and without the pretreatment respectively. The axis of ordinate shows an amount of produced digestion gas and the axis of abscissa shows digestion days.
It may be obviously understood that the anaerobic digestion treatment with the pretreatment makes the liquefying term of the sludge short and causes the increase of gas producing speed and an amount of produced gas. The composition of digestion gas which was produced by the anaerobic digestion with and without the pretreatment consisted of CH4 of 84.5% and CO2 of 15.5%, and CH4 of 84.6% and CO2 of 15.4% respectively ignoring the existance of N2 and H2). There was almost no difference between the digestion gases produced with and without a pretreatment.
Furthermore, viscosity of the sludge after pretreated and neutralized was 15 cp (centipoise) and viscosity was 23 cp without the pretreatment.
Surplus activated sludge which was remainder upon an urbane sewage treatment was concentrated so that its solid density became 8.6%. After that the sludge was diluted with water, to obtain five parts of sludge of 300 g of which solid density was in range of 1 to 5% and which content of organic material was 65%. Then hydrochloric acid of 35% was added to the parts of sludge, so that pH of the sludge parts was adjusted to 2.0 in a container. During said process the sludge was stirred. The sludge was heated at 100° C. during five minutes. Then, the sludge parts were cooled and sodium hydroxide of 30% was added to the sludge to adjust pH of the sludge to 6.9. Viscosity of those pretreated sludge parts was measured by a revolution viscometer.
The measure results of said experiments are shown in Table 1.
TABLE 1______________________________________ Solid Density % (wt/wt) 1 2 3 4 5______________________________________With Pretreat- CP CP CP CP CPment 6 20 110 300 620Without Pre-treatment 7 26 145 2,000 5,600______________________________________
When the solid density of sludge was under 3%, both values of viscosity as shown in Table 1 were not much different. When, however, the solid density of sludge was over 4%, both values of viscosity were remarkably different.
Usually upon digestion treatment, it is desirable to increase density of sludge for rise of treatment efficiency. However, in a case that the pretreatment of sludge is not provided, the sludge is in a state of paste that the observed value of viscosity of the sludge becomes higher. When liquid with high viscosity is stirred, stirring power of a digestion tank is required in proportion to the value of viscosity. As above mentioned, the invention can decrease the value of viscosity of sludge. Accordingly, the stirring power can be remarkably reduced upon digestion treatment.
Hydrochloric acid of 4.6 ml, of which density was 35%, was added to surplus activated sludge of 1000 g which was remainder of urban sewage treatment. The solid density of tie sludge was 3% (wt/wt) and the density of organic material was 2.0% (wt/wt). The sludge was stirred and the pH of the sludge was adjusted to 2.0. The sludge was continuously introduced into a stainless hose with an inner surface coated with epoxy resin and soaked in hot water at 98° C. for five minutes. The load of organic material was 32.3 g/l.day. Following that, the treated sludge was thrown into a cylindrical stainless liquefying tank of 10 l provided with a stirrer, a jacket, and an automatic pH controller in a state of said load of organic material. At this time, the stirring speed was 180 rpm and the temperature was 42° C. Sodium hydroxide was added to the sludge, so that pH became 5.8. Continuously liquefying treatment was made for four days. After the liquefying treatment, the sludge was thrown into a cylindrical stainless digestion tank of 20 l provided with a stirrer, a jacket and an automatic pH controller. At this time, the stirring speed was 180 rpm and the temperature was 40° C. Sodium hydroxide was added to the sludge for neutralization, so that pH became 7.4. Anaerobic sludge was added to the sludge and continuous anaerobic digestion treatment was made to produce methane gas for eight days. The remainder produced was introduced into a separator of b 2 l and kept for one day for separating into liquid and digestion sludge containing bacteria producing gas. For comparison, the liquefying and digestion treatments were made without a process of adding acid and heating.
The results of said experiments were as shown in Table 2
TABLE 2______________________________________ Amount of Produced Content of CH4 Rate of Digestion Gas in Digestion Digestion ml/g organic material gas (%) (%)______________________________________WithoutPretreatment 410 72 55WithPretreatment 478 74 63______________________________________
Surplus activated sludge which was remainder upon a treatment against water wasted from the food industries was concentrated by a centrifuge so that its solid density became 10%. After that, the sludge was diluted with water, whereby a sludge of 600 g of which solid density was 5% and the content of organic material was 60% was prepared. Then, a little amount of sulfuric acid was added to each part of the divided sludge, which was stirred, so that the sludge parts of which pH were 2, 3 and 4 were adjusted. Each part of sludges was introduced into a stainless autoclave with an inner surface coated with teflon and provided with an inner jacket, an outer jacket and a stirrer. Each part thereof was stirred and heated through entering super-heated steam into the jackets under the conditions shown in Table 3. After the heating treatment, cooling water was entered into the jackets. For each part, a measure was taken of the viscosity by a revolving viscometer. Following that, sodium hydroxide of 30% was added while stirring the sludge parts so that the pH was adjusted to 7.0. These sludge parts were thrown into a digestion tank respectively and anaerobic digestion sludge of 4% (wt/wt) was introduced into the tank as a seed sludge. Gas in a chamber of the tank as replaced with N2 gas. After that, each sludge was stirred at 150 rpm and made digestion treatment at 40° C. For comparison, sludge of 600 g of which solid density was 5% was adjusted to a pH of 6.9 without the pretreatment and added anaerobic sludge as seed sludge. Thus digestion experiment was made.
The results of those experiments are shown in Table 3.
TABLE 3______________________________________Condition ofPretreatment Temper- Heat Observed Term Required Amount of ature time Viscosity for Digestion producedpH (° C.) (min.) (cp) (days) CH2 (l)______________________________________1.0 100 5 2,000 22 7.0060 1 2,900 26 6.51 100 1 2,700 24 6.802.0 170 1 500 20 7.01 170 20 500 -- -- 170 30 500 47 2.103.0 100 1 2,300 25 6.7550 1 5,000 39 5.0560 1 3,000 30 6.203.5 100 5 1,500 24 7.03 160 10 1,000 27 6.90 170 1 1,300 23 7.00 170 20 1,100 45 3.8060 1 5,800 39 5.104.0 170 20 3,000 40 4.01 Without6.8 Pretreatment 6,000 42 5.04______________________________________
Domestic garbage with added water was crushed by a mixer, so that slurry of which solid density was 1.5% and which content of organic material was 7.0% was prepared. The slurry was stirred and hydrochloric acid of 2.4 ml of which density was 35% was added to the slurry so that pH was adjusted to 2.0. The slurry was heated in an autoclave. Temperature rose up to 130° C. in five minutes and held at the same for five minutes. After that the slurry was gradually cooled to 95° C. and then taken out from the autoclave and rapidly cooled in a fluid containing water and ice. Following that, sodium hydroxide of 3.0 ml of which denisty was 20% was added to adjust pH to 7.2. The adjusted slurry was thrown into a digestion tank and anaerobic sludge of 2% wt/wt as an added anaerobic seed for anaerobic digestion treatment. The solid density of the slurry was 3.1% and the content of organic material was 1.7%. The slurry was stirred at 200 rpm and underwent digestion treatment at 40° C. For comparison, slurry without the pretreatment was adjusted to a pH of 7.2 with sodium hydroxide and underwent digestion treatment at 40° C. The results of the above mentioned experiments are shown in Table 4.
TABLE 4______________________________________ Observed Required Viscosity Term Amount of Produced CP (days) CR, (1)______________________________________Digestion withPretreatment 3,000 31 8.1Digestion with-out Pretreatment 5,200 42 6.5______________________________________
While several preferred embodiments of the present invention have been set forth along with specific examples for purposes of illustration, further embodiments, variations and modifications are contemplated according to the broader aspects of the present invention, all as determined by the spirit and scope of the following claims.
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US1963581 *||Mar 21, 1932||Jun 19, 1934||Dorr Co Inc||Sewage treatment|
|US1997252 *||Jan 2, 1931||Apr 9, 1935||Dorr Co Inc||Sewage sludge treatment|
|US3105041 *||Sep 9, 1960||Sep 24, 1963||Genter Albert L||Sewage sludge digestion process|
|US3459659 *||Mar 13, 1968||Aug 5, 1969||Wilson & Co Inc||Waste treatment process and apparatus|
|US3649534 *||May 15, 1970||Mar 14, 1972||Du Pont||Wet oxidation of acidified activated sludge|
|US3772191 *||Apr 26, 1971||Nov 13, 1973||Thorn W||Method of digesting and further processing fresh sewage sludge or sopropel|
|US3959125 *||Apr 21, 1975||May 25, 1976||Sterling Drug Inc.||Treatment and disposal of sewage sludge|
|US4067801 *||May 12, 1976||Jan 10, 1978||Hitachi, Ltd.||Process and system for anaerobic treatment of biochemical waste|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US4491522 *||Nov 15, 1983||Jan 1, 1985||Agency Of Industrial Science & Technology||Anaerobic digestion process for organic wastes|
|US4609469 *||Oct 22, 1984||Sep 2, 1986||Entenmanns, Inc.||Method for treating plant effluent|
|US4632758 *||Sep 6, 1985||Dec 30, 1986||Commonwealth Engineering & Technology, Inc.||Anaerobic wastewater treatment system|
|US4666605 *||Oct 17, 1985||May 19, 1987||Shimizu Construction Co., Ltd.||Methane fermentation process for treating evaporator condensate from pulp making system|
|US4684468 *||Jan 29, 1986||Aug 4, 1987||Ateliers De Constructions Electriques De Charleroi||Process and installation for anaerobic digestion|
|US4885094 *||Mar 9, 1988||Dec 5, 1989||Micro Pure Systems, Inc.||Anaerobic digestion process, and forced fed fast rate digester|
|US4911843 *||Dec 9, 1988||Mar 27, 1990||Davis Water And Waste Industries, Inc.||Process for removal of dissolved hydrogen sulfide and reduction of sewage BOD in sewer or other waste systems|
|US4976864 *||Oct 6, 1989||Dec 11, 1990||Eniricerche S.P.A.||Treatment of the effluents from the production of epoxy resins|
|US5015384 *||Dec 4, 1989||May 14, 1991||Burke Dennis A||Anaerobic digestion process|
|US5076927 *||Mar 9, 1988||Dec 31, 1991||Hunter Robert M||Biocatalyzed partial demineralization of acidic metal sulfate solutions|
|US5310485 *||Sep 30, 1992||May 10, 1994||Darling-Delaware Company, Inc.||Process for dissolved gas flotation in anaerobic wastewater treatment|
|US5540847 *||Jul 26, 1994||Jul 30, 1996||Stultz; Jeffrey H.||Sludge digestion|
|US5593590 *||Feb 27, 1992||Jan 14, 1997||Technoagrar Consulting Ag||Process for separate treatment and disposal of mixtures of solid and liquid, organic wastes|
|US6391202 *||Jul 2, 1999||May 21, 2002||Michael Knobloch||Process and apparatus for treating wastewater from oil plant processing and cereal processing|
|US6855254 *||Dec 19, 2003||Feb 15, 2005||Shalom Recycling Inc.||Magerle metal waste recovery process|
|US6929744 *||May 2, 2001||Aug 16, 2005||United Utilites Plc||Sludge treatment at a mesophilic temperature|
|US7087172||Nov 4, 2003||Aug 8, 2006||Usfilter Corporation||Methods for reducing nitrate demands in the reduction of dissolved and/or atmospheric sulfides in wastewater|
|US7138049||Jul 7, 2005||Nov 21, 2006||Usfilter Corporation||Apparatus for reducing nitrate demands in the reduction of dissolved and/or atmospheric sulfides in wastewater|
|US7186341||Apr 24, 2006||Mar 6, 2007||Siemens Water Technologies Holding Corp.||Methods and apparatus for reducing nitrate demands in the reduction of dissolved and/or atmospheric sulfides in wastewater|
|US7285207||Jul 7, 2005||Oct 23, 2007||Siemens Water Technologies Holding Corp.||Methods and apparatus for reducing nitrate demands in the reduction of dissolved and/or atmospheric sulfides in wastewater|
|US7326340||Jun 9, 2005||Feb 5, 2008||Siemens Water Technologies Holding Corp.||System for controlling sulfide generation|
|US7435349 *||Mar 14, 2006||Oct 14, 2008||Industrial Technology Research Institute||System for treating wastewater containing organic compounds|
|US7553420||Sep 21, 2007||Jun 30, 2009||Siemens Water Technologies Corp.||Systems and methods for wastewater odor control|
|US7799215||Jun 30, 2009||Sep 21, 2010||Siemens Water Technologies Corp.||Wastewater treatment systems|
|US7799224||Jan 30, 2008||Sep 21, 2010||Siemens Water Technologies Corp.||Wastewater treatment methods|
|US7968057||Nov 23, 2005||Jun 28, 2011||Estech Europe Limited||Autoclave|
|US7972532||May 15, 2009||Jul 5, 2011||Siemens Industry, Inc.||Composition for odor control|
|US8092680||Oct 27, 2008||Jan 10, 2012||Landmark Structures I, Lp||System and method for anaerobic digestion of biomasses|
|US8430112||Jul 13, 2010||Apr 30, 2013||Siemens Industry, Inc.||Slurry feed system and method|
|US8480901||Jan 9, 2012||Jul 9, 2013||Landmark Structures I, Lp||Methods and products for biomass digestion|
|US8911627||Jul 8, 2013||Dec 16, 2014||Landmark Ip Holdings, Llc||Systems and method for biomass digestion|
|US8968646||Feb 21, 2012||Mar 3, 2015||Evoqua Water Technologies Llc||Synergistic methods for odor control|
|US20030155295 *||May 2, 2001||Aug 21, 2003||Son Le||Sludge treatment at a mesophilic temperature|
|US20040173525 *||Nov 4, 2003||Sep 9, 2004||United States Filter Corporation||Methods and apparatus for reducing nitrate demands in the reduction of dissolved and/or atmospheric sulfides in wastewater|
|US20050224409 *||Jun 9, 2005||Oct 13, 2005||Usfilter Corporation||Method and apparatus for controlling sulfide generation|
|US20050242010 *||Jul 7, 2005||Nov 3, 2005||Usfilter Corporation|
|US20050242011 *||Jul 7, 2005||Nov 3, 2005||Usfilter Corporation|
|US20060006121 *||Jul 8, 2005||Jan 12, 2006||Simpson Gregory D||Synergistic composition and method for odor control|
|US20060186040 *||Apr 24, 2006||Aug 24, 2006||Hunniford David J|
|US20060243661 *||Mar 14, 2006||Nov 2, 2006||Industrial Technology Research Institute||System for treating wastewater containing organic compounds|
|US20070241062 *||Jul 8, 2005||Oct 18, 2007||Simpson Gregory D||Synergistic composition and method for odor control|
|US20080041785 *||Sep 21, 2007||Feb 21, 2008||Siemens Water Technologies Corp.||Systems and methods for wastewater odor control|
|US20080253946 *||Nov 23, 2005||Oct 16, 2008||Estech Europe Limited||Autoclave|
|US20090250389 *||May 15, 2009||Oct 8, 2009||Siemens Water Technologies Corp.||Composition for odor control|
|US20110233146 *||Sep 29, 2011||Siemens Water Technologies Corp.||Synergistic wastewater odor control composition, systems, and related methods therefor|
|USRE36651 *||May 9, 1995||Apr 11, 2000||U.S. Filter Distribution Group, Inc.||Process for removal of dissolved hydrogen sulfide and reduction of sewage BOD in sewer or other waste systems|
|USRE37181||Nov 24, 1998||May 22, 2001||U.S. Filter Corporation||Process for removal of dissolved hydrogen sulfide and reduction of sewage BOD in sewer or other waste systems|
|CN103011542A *||Dec 13, 2012||Apr 3, 2013||清华大学||Anaerobic digestion device and process for pre-treating sludge with high solid content by heating method|
|WO1992020628A1 *||May 10, 1991||Nov 26, 1992||Dennis A Burke||Anaerobic digestion process|
|U.S. Classification||210/613, 71/10, 48/197.00A, 210/631, 210/603|
|International Classification||C02F3/28, C05F7/00, C12N1/00, C02F11/04, C02F1/02|
|Cooperative Classification||C02F1/02, Y02E50/343, C02F3/286, Y02W30/47|
|European Classification||C02F3/28S, C02F1/02|