DE2930812A1 - ARRANGEMENT FOR THE TREATMENT OF ORGANIC WASTE, WASTEWATER AND THE LIKE - Google Patents

Description

ALEXANDER R. HERZFELD 6 Frankfurtα.μ.θο

LAWYER ZEPPELINALLEE 71 OQODQ 1 O THE LANDGERICHT FRANKFURT AM MAIN TELEPHONE 0611/779125 £. & ■ $ \ J \ J \ fm

Applicant: Corning Glass Works
Corning, NY, USA

^ZVL arrangement ? Treatment of organic waste, sewage and the like

The invention relates to an arrangement for processing organic Waste in liquid medium, sewage and the like.

Organic waste, including industrial and agricultural Waste has been polluting in the past Wisely eliminated, e.g. in rubble dumps, as an embankment, by lowering on the high seas, etc.

The endeavor therefore goes to a processing of the organic waste, with recoverable products at the same time, or the waste from energy production can be harnessed.

This subheading includes treatment processes by biological, aerobic or anaerobic permentation, thermophilic aerobic digestion, destructive distillation including hydrocarbonization and pyrolysis, incineration, etc.j see WJ Jewell et al., "Methane

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Generation from Agricultural Wastes: Review of Concepts and Future Applications ", Paper No. NA74-107, etc. presented in 1964 on the occasion of the Northeast Regional Meeting of the American Society of Agricultural Engineers, West Virginia University, Morgantowm, West Virginia, August 18-21, 1974.

The "biological treatment" appears to be the most promising especially through anaerobic fermentation. The anaerobic filter is essential for this, see J.C. Young et al. Jour. Water Poll. Control Fed., 41, R160 (1969); P.L. McCarty, "Anaerobic Processes," published on the occasion of the Birmingham Short Course on Design Aspects of Biological Treatment, International Association of Water Pollution Research, Birmingham, England, September 18, 1974; and J.C. Jennett et al., Jour. Water Poll. Control Fed., 4Y, 104 (1975).

Dieter anaerooe filter oejtjlt in, we.sentlic · - ^ * \ s> -i,. ,, ^ -.? oie ^ er. / from ρ or an S ", embedding, similarly -learning arrobea seepage filter, whereby the waste flow runs through the bed to the top and this is completely immersed in liquid. The anaerobic microorganisms gradually fill and form the spaces between the boulders or pebbles a large, active biomass, the discharge is essentially free of biological solids, see JC Young et al., op. cit., R 160.

This anaerobic filter is best for water soluble organic wastes, see J.C. Young, op. Cit., R160 and R171. aside from that longer retention times of the waste in the filter are required,

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BATH ORIGINAL

a greater decrease in the chemical oxygen demand of the To achieve waste. Depending on the characteristic oxygen demand of the waste, dwell times of 4.5 - 72 hours are required, to achieve a reduction in chemical oxygen demand of about 36.7-93.4%, J.C. Young, op. Cit., R167. Included Even these results were only achieved under optimal conditions for synthetic waste with balanced proportions Carbon, nitrogen, phosphorus and carefully adjusted pH levels.

The object of the invention is an arrangement for waste treatment which is also suitable for waste masses with pesticides in the waste stream and can handle waste without extensive preprocessing.

The object is achieved by the method of the invention in that that the first reactor is a hydrolytic redox bioreactor, containing a carrier material suitable for the accumulation of a biomass, and the second reactor is an anaerobic bioreactor with a porous, inorganic carrier suitable for the accumulation of a biomass.

Further favorable configurations can be found in the description and the claims.

Waste is referred to as biodegradable here, which contain at least a portion of biodegradable organic substances. Usually their share is at least

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SUBMITTEDJ " ^ '

50% by weight, but sometimes also considerably less. Necessary is just that for the necessary microorganisms toxic components miss.

The organic waste, possibly in an aqueous medium, can also contain non-biodegradable organic and inorganic substances if they are non-toxic to the microorganisms contained in one of the bioreactors.

The nature of the solvent is not inherently critical. It usually consists of at least about 50% by weight of water, and the water content is preferably 80-98 %.

In many cases, pretreatment of the waste stream is unnecessary. Occasionally, however, a dilution with water, the removal of excessive amounts of pesticides or coarse particles to maintain the price of the pumps, or to increase the pH value by adding an organic or inorganic base such as potassium carbonate, Sodium hydroxide, triethylamine and the like are desirable or even be required. Pest or non-aqueous or non-liquid waste can be caused by adding water to the best consistency can be diluted.

The term "bioreactor" (biochemical reactor) means that living microorganisms undergo chemical transformations or changes cause. In immobilized bioreactors, these microorganisms are in an immobilized state.

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Both reactors of the method and the device of the invention contain one suitable for the accumulation of a biomass porous, inorganic carrier. In the case of the second reactor, it is regulated in an inorganic hydrophobic membrane Pore size provided.

Required but practically, the inorganic support is of the same type in both reactors, and preferably consists of a porous, inorganic large-area support with the ability to hold a large biomass in a relatively small volume. Particularly preferred are carriers whose pores have a minimum diameter of at least 70% of the size of the smallest main dimension, but smaller than about five times the largest main dimension of the microorganisms present in the reactor. Average pore diameters of around 0.8-220 μm are most favorable.

Carriers with a surface area greater than about 0.01 m 2 / g carrier are regarded as "large-area" carriers. The surface is usually made by adsorption of an inert gas, or according to the so-called B.E.T. Method (S.J. Gregg and K.S.W. Sing Adsorption, Surface Area and Porosity ", Academic Press, Inc., New York, 1967), while the pore diameters are the simplest determined by mercury penetration; s. N.M. Winslow and J.J. Shapiro, "An Instrument for the Measurement of Pore-size distribution by mercury penetration; ASTM Bulletin No. 236, February 1959.

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The inorganic carrier usually consists of silica-containing or silica-free amorphous or crystalline material. Examples of silicic acid-containing substances are glass, silica, halloysite, kaolinite, cordierite, wollastonite, bentonite and the like. Examples of silicic acid-free substances or metal oxides are aluminum oxide, spinel, apatite, nickel oxide, titanium oxide and like that. Mixtures of both types are also possible, such as aluminum oxide - cordierite. Clays are also particularly cheap, such as halloysite, kaolinite and cordierite. For details, see U.S. Patent 4,153,510.

The porous support not only allows a large biomass to accumulate in a small space, but also holds the biomass also in the reactor.

Suitable microorganisms and their derivatives are all organic substances that break down or use as nutrients themselves, or in Form of the metabolites or metabolic products of other organisms using microorganisms such as algae, bacteria, mold, yeast and the like. Preference is given to bacteria, molds, as well as yeasts, and bacteria appear most favorable.

In addition, the type of bacteria used in the individual case is not of critical importance as long as the one aimed at in the individual case Accumulation of the biomass is achieved. It consists of one or more species that are not necessarily identified or must be known.

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Furthermore, it is not necessary for the biomass in the bioreactors to be exclusively aerobic or exclusively anaerobic is; it suffices if its main function, (at least 50 96) the of a hydrolytic redox bioreactor or that of an anaerobic bioreactor.

This also means that the boundary line between the two systems is not critical and not always in the middle between must run in both bioreactors and also by changing and adjusting the oxygen content dissolved in the wastewater or can be regulated. There is usually no need to alter the natural oxygen content of the waste stream.

The task of the "hydrolytic" redox bioreactor is to break the existing macromolecules into smaller units, monomers and Oligomers, split by hydrolysis and oxidation-reduction reactions. As a result, this bioreactor also reduces the content dissolved oxygen of the aqueous medium.

This first bioreactor is not an "aerobic" bioreactor in the conventional one Senses. The aqueous medium is not constantly aerated or even saturated with air or oxygen. To be there However, if the residual oxygen content is depleted, at least part of the oxidation - reduction takes place in an aerobic manner.

Examples of those suitable for the hydrolytic redox bioreactor As strictly aerobic bacteria, microorganisms are the species Pseudomonas fluorescens, Acinetobacter calcoaceticus and the like;

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as facultative anaerobic bacteria species such as Esciierichia coli, Bacillus subtilis, Streptococcus faecalis, Staphylococcus aureus, Salmonella typhimurium, Klebsieila pneumoniae, Enterobaeter cloacae, Proteus vulgaris and the like, anaerobic bacteria such as Clostridium butyricum, Bacteroides frazilis, Fusobacterium necrophorum, Leptotrichia buccalis, Veillonella parvula, Methanobacterium formicicum, Methanococcus mazei, Methanosarcina barkeri, Peptococcus anaerobius, Sarcina ventriculi and the like, molds such as Trichoderma viride, Aspirgillus niger and the like, yeasts such as Saccharomyces cerevisiae, Saccharomyees ellipsoideus and the like.

Examples of the microorganisms of the anaerobic bioreactor include the anaerobic and facultative anaerobic bacteria mentioned above and yeast. Naturally, the anaerobic bioreactor should not contain exclusively strictly aerobic bacteria; as part of it their presence usually harmless.

The selection is primarily based on the desired results or products, or if no specific product arises should, in terms of the efficiency of the waste treatment or operating conditions such as temperature, throughput and the like, availability and stability or persistence of the microorganisms and the like. Should, however, be a specific product are generated, the selection is made more with a view to product maximization. The following table contains a few Examples for the production of certain products of suitable microorganisms of the two bioreactors.

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Hydrolytic redox bioreactor Anaerobic bioreactor

product

Acetobacter aceti Acetobacter peroxydans Aoetobacter pasteurianus Propionibacterium acidi-propionici Bacillus maierans Bacillus acetoethylicus Erwinia dissolvens Escherichia coli Klebsiella pneumoniae Trichoderma viride Aspirgillua niper Saccharomyces cerevieiae Saccharomyces ellipsoideus AspergilluB ni ^ he Trichoderma viride, Escherichia col i methanobacterium Soehn ^ Enii methanobacterium formicicum Methanococcus mazei methanobacterium thermoautrophicum i "iu ö i'j.arj.o bact ε r i am r amiuan t ium Methanopacterium mobile Methanoaarcina methanica Methanosarcina barkeri Methanococcus mazei Methanococcus vannielii

Propionibacterium acidi-propionici Saccharomyces cerevisiae Saccharomyces allipsoideus Clostridium propionicum Clostridium saccharoacetoper-butylicum

Clostridium butyricu m

methane

methane

methane

methane

'-.ethane

methane

methane

methane

methane

methane

methane

Ethanol

Ethanol

Propanol

Butanol

hydrogen

OD CO O OO

The microorganisms are usually introduced into the reactors in a known manner. So the reactor, for example in Ways of passage through a liquid or aqueous suspension of microorganisms, or the microorganisms are "inoculated" are added to the wastewater stream. If this already contains the species in question, the necessary colonies of organisms arise when the wastewater flows through the reactor mostly by itself. The carriers can also be immobilized on them Microorganisms are used in the bioreactors.

The design of the two bioreactors is also not critical; The simplest are, for example, the cylindrical or tubular once-through reactors of the examples below. These are open on both sides and contain the inorganic carrier. For example, the cylinder consists of one for the used Gas and liquid impermeable material, such as glass, stainless steel, glass-coated steel, polytetrafluoroethylene and the same. The bioreactors can be provided with a jacket, e.g. made of the specified material.

Each reactor usually contains one or more channels for the passage of a fluid medium; with multiple channels they are separately or connected in series. The inorganic support can be arranged in or around these channels. in the In the example of the cylindrical reactor, it is located in the cylinder tube or, if a jacket is provided, between this and the cylinder, the liquid then flowing through or around the cylinder, in the latter case in the second

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Reactor then gas products are withdrawn from the cylinder.

Known means are suitable for withdrawing gaseous products. Mostly you can e.g. connect the second bioreactor to one Vacuum can simply be pumped out.

The process temperatures are only critical insofar as the microorganisms must remain viable in the reactors.

In practice, temperatures of about 10-60 ^° C. are possible. Under normal conditions, the first bioreactor is preferably kept above ambient temperature, about 30-40 ^° C.

As already mentioned, the waste stream can be introduced into the arrangement without pretreatment. Whether a pre-treatment is carried out will mainly depend on the expected result, in the case of some examples below, if significant reduced oxygen demand and methane as the main product is desired. If the methane is to be used as fuel, then it is it is advantageous to let as few gaseous by-products as possible, such as carbon dioxide, arise. A default setting of the the waste stream to be treated must be at pH 8 or higher, reducing the carbon dioxide generated by the microorganisms in solution remains.

The following examples, with reference to FIG. 1 of the drawing, serve for further explanation without limitation. All

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Temperatures are in ⁰ C. The wastewater is pumped with a pump 3 from the container 2 via the rubber pipes 5 and 7 and the pressure gauge 6 in the line 7 into the hydrolytic redox bioreactor. This reactor consists of an inner tube made of glass 8, which is enclosed and sealed in a glass jacket 9. The inner tube contains a carrier suitable for the accumulation of a biomass, for example according to US Pat. No. 4,153,510. The glass jacket is connected to a constant temperature water bath 12 in a sealing manner via a rubber tube. The waste material, waste water and the like are passed from the hydrolytic redox bioreactor into the anaerobic bioreactor 13 through a rubber line 14 connected to both bioreactors. This consists of a glass jacket 15 which contains an outlet opening 16 and is partly filled with further inorganic carrier material 10 and closed at both ends. The rubber tube 17 connected to the outlet opening of the jacket leads to the pump 18, which pumps the gases (methane) produced from the space enclosed by the jacket and into a suitable collecting container, for example an inverted water-filled bottle. The glass jacket of the anaerobic bioreactor is equipped with several liquid level sensors 20 which are connected to a controller 21 for the pump. The outlet 22 flows through the rubber tube 23 into the anaerobic bioreactor, which contains a throttle valve 24, and from there into a receiving vessel 25.

example 1

The pump 3 consisted of a fluid metering pump (Fluid Metering Inc., Oyster Bay, N.Y., USA), which was connected via a 35.5 cm long rubber tube

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-Yf-

• Ab-

connected to the hydrolytic redox bioreactor. At the inlet end of the pump was a 50 cm long, with a waste container connected rubber pipe connected. In the connecting pipe between the pump 3 and the bioreactor 4 was a pressure gauge intended.

The hydrolytic bioreactor consisted of a Pharmacia type column K 16/20 (Pharmacia Fine Chemicals, Uppsala, Sweden) with a water jacket with a constant temperature water bath was connected. 24.5 g of a support made of cordierite with an average pore diameter of 3 μm and a pore size were placed in the column chmes server division 2 - 9 / um given.

The anaerobic bioreactor consisted of a 250 χ 15 mm column of the Lab-Crest type. Approximately 125 mm of the inner cylinder has been removed, so that the jacket formed the actual bioreactor, which the end pieces of the inner cylinder sealed on both sides. The bioreactor was occupied with 51 g of the aforementioned cordierite support and placed horizontally.

Both bioreactors were connected to one another with a 10 cm long piece of rubber tubing. The total volume of fluid in the pump that Lines and the bioreactors was 120 ml. One of the openings the anaerobic bioreactor jacket was closed with a Tygon pipe socket and the pipe was clamped. The other end was on a peristaltic Buchler pump (Buchler Instruments, Port Lee, N.Y., USA) connected with a thick-walled Tygon tube.

030050 / Ό574

This arrangement was set up in the following way: The pipe coming from the pressure gauge was disconnected from the inlet of the hydrolytic redox bioreactor and the free end connected to the pipe coming from the anaerobic bioreactor of a corresponding arrangement. With the supply of sewage, the The system coupled in this way operated for 13 days. The gas developed in the anaerobic bioreactor was converted into The gas evolution rate is collected in a cylinder placed upside down in a flat, water-filled container Measured daily and the gas measured by mass spectrometry. By known colorimetric dichromatic oxidation methods the biological oxygen deficiency requirement (GOD) of the initiated Periodically determined wastewater and the runoff from the anaerobic bioreactor. Table I contains the measured values.

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030050/0574

TABEL

Day

β approx ο ο οι ο

1 2 5 6 7 8 9 13

Throughput
ml / hour Gas development
ml / hour 31 2.3 37.1 5.7 32.8 6.8 37.2 1.2 47.3 3.4 36.9 3.4 32.2 4.2 35 * 9 2.0

Gas composition (ΜοΙ, -%

CO,

91 ,1 3.2 0.3 5.2 0.1 bfc , 0 4.0 1.3 28.3 0.5 70 , 3 2.5 1.6 24.8 0.4 90 , 6 2.4 0.4 6.5 0.2 88 ,1 2.2 0.4 9.1 0.2 84 , 2 2.7 0.1 12.7 0.3 78 , 4 0.8 0.3 20.0 0.4

CD CO O OO

-γί-

The arrangement was then further appropriate in front of d-3r The arrangement is separated and the pipeline from the pressure gauge is reconnected to the inlet of the hydrolytic redox bioreactor, and so run separately, with waste water of pH 8.6 8.9 (with aqueous sodium hydroxide) being introduced. Table II contains the operating conditions and gas composition, Table III the results and carbon calculations.

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X AJ5 £ jJJJJUi 11

Day throughput gas evolution pressure pH of gas composition in mol% remarks

ml / hour ml / hour psi inlet outlet CH ₄ GO ₂ O ₂ N ₂ A

8.6 8.5 81.2 1.6 0.1 16.7 0.4

8.0 8.0 42.3 2.5 2.2 52.1 0.9. a

8.4 8.1 - b

8.0 8.2 61.9 1.6 0 35.8 0.7

0 8.6 8.1 _____

0 8.1 8.1 64.1 1.3 0.1 33.9 0.6 c

2 8.0 8.4 _____

1.4 8.2 8.6 69.5 1.1 0.6 28.3 0.5 - £ χ>

1.0 - - 75.6 1.4 0.8 21.9 0.4

1.2 - - 74.8 1.0 0 23.7 0.5

1.5 8.4 8.2 81.8 1.9 0.1 15.9 0.3 1.2 8.5 8.1 83.6 1.6 0.1 14.5 0.3 1.2 8.1 8.0 82.0 1.8 0.1 15, & 0.4 1.0 6 ,; c., 1 82.5 3.4:: ■ I3, c 0.2

1.4 8.6 8, b -J1.1 4.3 0 4, ή 0.1 - £>

CaJ O OO ι

14th 37.7 2.9 15th 41.4 0.1 16 37.3 - 19th 16.3 0.4 20th 41.4 0 Cj IZ 20.3 0.6 O 13th 9.9 0 Cri
O Si 9.8 1.1 G
Cn
-J ^ 25.0
22.6 0.4
0.6 20.3 1.1 30th 28.2 3.9 33 31.2 1.6 34 <6.0 2.5 35 4.0 4.9

TABLE II (continued)

Day throughput gas evolution pressure pH of the gas composition in mol% remarks ml / h. ml / hour psi inlet outlet CH. CO ₉ O ₉ N ₉ A

~ T ^ - ι - ι „ ι ι

6.5 1.2 8.6 8.3 93.8 3.9 0 2.2 0.1

8.3 1.1 8.6 b, 5 94.1 3.7 0 2.1 0.1

2.5 1.7 8.4 8.4 92.4 4.6 0 2.8 0.1

6.9 1.9 8.5 8.1 93.2 3.8 0.1 2.8 0.1

5.5 1.6 8.6 8.2 93.9 2.7 0 3.3 0.1

17.9 1.5 8.3 8.0 83.5 3.7 1.7 10.9 0.2

10.1 1.4 8.6 8.1 93.6 3.9 0 2.3 0.1

2.2 2.0 8.0 8.6 87.7 6.2 0 6.1 0.1 - fcj

4.5 1.0 8.0 8.0 t 8.7 4.8 0 6.4 0.1 -

9.1 1.5 8.5 8.0 92.7 4.3 0.1 2.8 0.1

15.5 1.6 8.4 Li, C) 92, ο 5.5 0 5.6 0.1

² »9 1.2 8.6 8.3 66.3 5.9 0.1 5.6 0.1 d

% ² 1.0 8.4 8.2 91.8 4.8 0;?, 3 0.1

⁵ » ² 1» 9 8.6 8.3 93.3 4.8 0.1 1.3 0.1 - * £

^1Ü » ² '1» ⁶ 8.4 8.2 93.1 4.2 0 2.6 0.1 - q

36 19.0 37 10.0 40 13.9 41 18.6 42 28.4 O 43 30.5 CJ O 44 28.3 O cn
O 47 7.8 ό 48 22.2 cn -α 49 22.8 ** » 50 21.8 51 10.1 54 - 55 4.1 56 22.5 57 35.9

TABLE II (continued)

Day throughput gas evolution pressure pH des / /

ml / hour

ml / hour

psi inlet outlet GH

Gas addition in mol% Remarks

GO

58 36 ,8th 62 48 , 0 104 - 106 31 , 9 107 27 , 2 O CJ
ο 110 26th , 4 O 111 28 , 3 O ■ * ">
O OI

22.6

13.5

12.6

12.4

4.1

12.6

1.5 3.2 8.1 92.8 3.8 0 3.3 0.1

2.4 8.4 8.2 92.4 2.5 0.1 4.9 0.1

1.0 8.5 8.3 94.0 2.7 0 3.1 0.1

1.0 8.6 8.2 95.2 2.4 0 2.4 0.1

1.0 8.1 8.1 92.2 3.1 0.3 4.2 0.1

1.0 8.5 8.0 92.0 2.8 0.2 4.5 0.2

ΙΌ CD CO

O '

OO

^a 'The gas pump was removed and the gas transport was only effected by the pressure of the anaerobic bioreactor.

'The temperature of the water bath was increased from room temperature to 30 ⁰ G; A check valve was inserted into the end of the line leading out of the anaerobic bioreactor.

^c 'Instead of one, three check valves were used. 'The check valve was clogged and has been cleaned.

° e)

<* »'Since it was difficult to adapt the gas discharge quantities to the feed-in values, weras

ο a liquid level regulator connected to the anaerobic bioreactor in order to: -

Keep the skill level at 60 % of the deduction. The switching function of the controller was transferred to the

^ Feed pump connected.

^ j 'The arrangement was switched off and kept at room temperature for 42 days.

^ 'The operation was resumed and the temperature of the water bath set to 31 ⁰ O. The hold function of the liquid level controller was separated from the feed pump and connected to the gas pump. The three check valves were replaced by one check valve.

'The water bath temperature was raised to 40 ⁰ C.

TABLE III

Day COD (mg / 1)

Inlet-outflow-% decrease

Carbon (mg / 1) inlet drain -% decrease

CH * generated, released in % of C C volatilized

O CO O O cn ο

15th
20th IVJ
ro 1200 990 17.5 27 480 360 25.0 29 1100 600 45.5 34 3500 1500 57.1 36 2700 1500 44.4 41 2000 410 79.5 43 1800 660 63.3 48 790 410 48.1 50 1600 310 80.6 55 2100 250 88.1 57 1600 330 79.4 62 900 270 70.0 106 1850 730 60.5 111 1510 380 74.8

450 412 8.4 403 334 17.1 287 250 12.9 373 336 9.9 1398 709 49.3 969 662 31.7 712 311 56.3 658 391 40.6 448 330 26.3 651 348 46.5 745 305 59.1 576 303 47.4 371 245 34.0 680 454 33.2 571 303 46.9

39.8
54.3

39.1
37.5
29.3
38.4

98.1 116.0

82.4

110.5

88.0

81.9

ro co co ο

Example 2

Example 1 was repeated but the vehicle was Dura.lite Rouge (F. Guery, Ranbervi Hers, France) with a Poreridur knife distribution from 0.4 - 6 µm, an average pore diameter of 4.5 / M, a pore volume of 0.4 ecm / g, and one Porous: f-'t of 51.5? &; the quantities I ^ hydrolytic redox-bioreal'tor and in the anaerobic reactor there were 22 p; or 52.5 g.

The arrangement was inoculated as in Example 1, but the water bath temperature was set to "" 51 C, and the coupled arrangement was operated for t days. A check valve was installed in the end of the drain line from the anaerobic reactor. The operation was observed for a further 33 days. Satisfactory operation did not begin until a ^v : i 40th day of operation (including the first 6 days in a coupled arrangement).

km 20th operating station; The check valve was replaced by three check valves.

Table IV contains the operating conditions and the gas composition From the 40th day of operation, Table V shows the corresponding results and carbon calculations.

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030050/0574

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030050/0574

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TABLE IV (continued)

Day feed gas evolution pressure pH of the liquid gas composition in mol .- $ Bemerrate ml / h. lung ml / hour psi inlet - outlet CH, GO ₂ Og N ₂ ^A kungen

15.7 18.0 21.5 23.3

22.6 2.0 8.6 7.7 93.5 6.1 0 0.3 0 b

17.2 2.0 10.0 7.7 83.1 14.9 0 2.0 0 c 19.4 2.5 7.2 7.7 ö 8.3 11.7 0 0 0 c

21.3 2.5 9.5 7.3 81.0 17.7 0 1.0 0 d

'Instead of just wastewater, I got wastewater with 1 YoI. -% of consumed sulphite solution introduced and Rait JaGH adjusted to pH 9 - 9.9. The sulphite content contributed to the GOD or total carbon content 2260 to 760 mg / 1.

'The sulphite content in the amount introduced was increased to 2.5 vol .- /!) And the pH was adjusted to 9.7, Contributions to GOD and total carbon were 5700 mg / l and 1900 mg / l, respectively.

^c ^ 0.22 % H ₂ S in the gas outlet.

^d ^ 0.3 % H ₂ S in the gas outlet. ^

. 57 25.2 60 21.1 61 24.1 62 25.9 63 23.6 030050 / 64
67
68 26.2
23.2
20.7 O
cn
»4
JN a) Instead of nu

2.0 7.2 2.2 7.7 2, υ 9.2 2.0 9.8 2.0 8.6 2.0 10.0 2.5 7.2 2.5 9.5

sequence CH ₄ GO ₂ ° 2 N ₂ ^A. 7.7 86.4 11.0 0 2.6 0.1 7.9 8ö, 4 8.1 0 3.5 0.1 7.9 92.0 5.3 0.1 2.5 0.1 7.9 92.0 6.0 0 1.9 0.1 7.7 93.5 6.1 0 0.3 0 7.7 83.1 14.9 0 2.0 0 7.7 over 8.3 11.7 0 0 0 7.3 81.0 17.7 0 1.0 0

TABEL

O Oi OO Ol O

lay COD
enema (mg / 1)
sequence % Abi 40 920 290 68.5 42 1800 1000 44.4 47 1400 430 69.3 49 780 220 71.8 54 240Ö 1500 37.5 56 2300 1500 34.8 61 6000 3400 43.3 63 6300 3600 42.9 68 8500 5000 41.2

Carbon (mg / 1) ^GH 4 ^ΘΓ2Θη ^ » ⁱⁿ #

Decrease in inlet drain % decrease 0 released C volatilized

365 213 41.6 706 391 44.6 578 322 44.3 284 162 43.0 889 644 27.6 834 638 23.5 2064 1493 27.7 1948 1275 .. ■ 34.5 2616 1911 26.9

32.1

31.0

15.7

14.1

21.3

24.6

'17, 1

72.7

72.1

57.1

60.0

77.0

71.3

63.3

CTv

K) CQ CO CD OO

Example 3

BeisTDiel 1 was repeated, but the carrier was Duralite Moire (P. Guery, Rambervillers, Prance), pore diameter distribution 0.8-30 / µm, average 6, ma, porosity 34.1 }, quantities 20 g and 50 g, respectively in the hydrolytic redox or anaerobic bioreactor. The arrangement was inoculated as in Example 2 for 10 days. A significant decrease in the biological oxygen requirement was not observed until the 34th day of operation. The tables (operating conditions and gas composition in Table VI, results and carbon calculations in Table VIl) begin with the 34th day of operation.

- 27 -

030050/0574

COPY

TABEL

Day

Expulsion gas evolution pH of the liquid Gas composition in mol .- ^ o Remarks

rate ml / h ml / hour Pressure inlet - outlet psi

GH,

00,

N,

tV>
00 34 11 35 25th 39 25th 40 32 ©
ω
O 41
48 35
24 &
m
ö
"S.
Ö
(Si
«4 49
52
53 19th
15th
22nd 54 21st 55 16 59 17th 60 18th 61 22nd 62 17th , 4 ,8th ,8th , 0 , 9
, 5 , 4
, 9
, 6 , 2 , 2 , 2 , 2 , 2

4, p ο. 8th, 5.0 0 8th 8.7 0 8th 10.0 0 8th 10.9 0 6th 7.1 0 8th 3.2 0 b 7.3 0 7th 10.9 0 8th 11.2 0 8th 8.6 0 8th 8.6 0 11.0 0 8th 13 0 0 8th , 7 , 7 , 7 , 5 , 6 .7 , 6 , 9 , 7 ,8th , 5 , 5 , 5 , 4 , 5 , 5 , 5 , 6 , 6 , 7 , 7 , 6 , 5 8.1 , 5 ,8th , 5 , 7

11.9

0.5 8.7

90.5 3.8

90.1 2.2

92.7 1.5

93.1 1.0

93.1 1.6

93.7 0.7 91.3 3.4 90.1 3.6 91.3 2.8 94.1 2.5

91.8 2.3 90.3 3.3 92.7 3.1

93.9 3.4

0 5.6 0.1

0.4 7.1 0.2

0.4 5.2 0.1

0.3 5.5 0.1

0 5.2 0.1

0.2 5.3 0.1

0.4 4.8 0.1

0.7 5.5

0.8 4.9 0.1

0.1 3.1 0.1

1.1 4.7 0.1

0.9 5.3 0.1

0.5 3.6 0.1

0.1 2.6 0.1 92.5 3.2 0.6 3.7 0.1

.ro

TABLE VI (continued)

Day feed gas evolution pressure pH of the liquid gas composition in moles -96 remarks

rate ml / h ml / hour

psx

Inlet - outlet CH,

CO,

67 25.9 69 23.1 70 25.9 74 19.3 75 19.3 O 0 » 76 21.4 & ©
cn 77 18.6 θ 80 7.0 ώ oil 81 26.9 Jr * 82 29.1 83 28.8 87 17.7 88 27.1

10.3

8.1

9.9

13.4

17.0

16.9

18.9

7.0

21.5

23.6

24.0

17.5 19.0

0.5 8.6 0.5 8.5 0.5 8.5 0.7 7.9 0.5 8.8 0.5 8.7 0.5 8.6 0.8 8.2 0.5 8.6 0.5 8.6 0.5 B, 7 0.9 8.4 0.5 8.5

7.9 8.1

7.8 8.4

8.0 8.0 7.8 8.2 7.8 7.7 7.9 8.1 7.7

90.1 2.4 0.7 6.8 0.1 91.7 2.2 0.7 5.3 0.1 90.4 2.6 0.4 6.4 0.1 91.7 5.1 0.1 3.0 93.4 4.1 0.3 2.2

93.2 3.7 0.5 2.7

93.3 4.5 0.1 2, U 91.2 5.0 0.3 3.0

93.7 3, ö 0.2 2.4

93.8 4.3 0.1 1.8 93.7 4.5 0.1 1.7 93.1 5.4 0.1 1.5 Ü 93, S) 4.1 0 2.0

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030050 / Ό574

- 30 -

BATH ORIGINAL

Example 4

Example 1 was repeated, but the carrier was insulating sciamotte (JM-23) from Johns-Hanville Corp., Denver, Colorado, USA), pore diameter distribution 2 - 15 / µm, more average Pore diameter 9 / um, pore volume 1 ccm / ^, porosity 6b; (,, 10. ;; bsv /. 1 i> g in hydrolytic redox bsw. anaerobic Ξ ^ ΐο-reaktnr; Imp fun fi as in example 1 for 7 days. Satisfactory Results were observed from day 29, but up to for the 37th 'Tat * leaks were sharing a problem. Table VIII The new operating conditions and the gas addition take place, Table IX shows the results and carbon calculations from the 29th tar ;.

Ö3QQ50 / 057A

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TABLE VIII (continued)

Day feed gas evolution pressure pH of the liquid gas composition in moles, -96 comments rate ml / h. lung ml / hour psi inlet - outlet CH ₄ GO ₂ O ₂ N ₂ A

56 58 59 65 66

O 69

ο 71

70

72 77

21.7 18.7 18.7 22.9 18.6 27.4 27.8

26.7 22.8 28.3

5.9

5.5

5.1 13.20 12.8

14.1 16.4 22.4 20.7 17.9

1.5 8.7 1.4 8.5 1.4 8.5 1.3 8.8 1.4 8.6 1.9 8.1 1.9 8.6 1.6 8.6 1.6 8.6 2.1 8.5

7.9 8.2 7.9 8.0 8.0 7.7 7.8 7.8 7.9 7.7

90.7 2.0 0.1 7.1

88.5 2.0 1.1 8.2

89.2 2.6 0.4 7.7

94.0 3.0 0.1 2.9

92.7 4.0 0.1 3.1

92.0 4.5 0.1 3.4

95.4 2.9

1.7

93.3 4.3 0.1 2.3 93.9 4.8 0 1.3

94.1 4.2

1.7

0.1

0.1

0.2

Water bath became inoperative; the redox hydrlytische - bioreactor was run at room temperature (20 ⁰ C).

Water bath started up again, temperature set to 31.5 ⁰ O.

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030050/0574

Claims (12)

Patentansprü cne Arrangement for processing biodegradable organic waste in a liquid medium, waste water and the like, im Passage through two or more reactors occupied with immobilized microorganisms, characterized in that the first reactor is a hydrolytic redox bioreactor containing a carrier material suitable for collecting a biomass and the second reactor is an anaerobic bioreactor with a porous, is an inorganic carrier. 2. Arrangement according to claim 1, characterized in that a gas discharge is connected to the anaerobic bioreactor. 3. Arrangement according to claim 1, characterized in that the hydrolytic Redox - bioreactor at a temperature of 10 - 60 ^0C, preferably 30 - 40 ⁰ C is maintained. 4. Arrangement according to claim 1, characterized in that the inorganic carrier of the anaerobic and / or the hydrolytic Redox bioreactor is a porous, large-area, inorganic, suitable for the accumulation of a large biomass in a small volume Carrier is. 5. Arrangement according to claim 4, characterized in that at least 70 % of the pores of the inorganic support diameter at least as large as the smallest main dimension 030050/0574 - 35 ORIGINAL INSPECTED • a · but smaller dan alts of the largest dimension of the main fünffaube vorhandt-NEN each comprise microorganisms. 6. Arrangement according to claim 4, characterized in that the average pore diameter of the inorganic support Is 0.8-220 / µm. 7. Arrangement according to claim 6, characterized in that the inorganic carrier consists of cordierite. 8. Arrangement according to claim 7, characterized in that the carrier has a pore size distribution of 2-9 / um, and average Has pore diameter of 4.5 / µm. 9. Arrangement according to claim 6, characterized in that the inorganic carrier is a halloysite or kaolin. 10. The arrangement according to claim 9 _f, characterized in that the inorganic carrier has pore sizes of the ranges 0.4 - 6 / um
Pore diameter distribution, 4.5 / µm on average, or 0.8 - 30 / µm pore diameter distribution, 6 / µm on average, or 2 - 15 / µm pore diameter distribution, 9 / µm on average, having. 11. Arrangement according to one of claims 1 - 10, characterized in that that the main effluent product of the anaerobic bioreactor Is ethanol. 030050 / Ό574 .3- 12. Arrangement no: one of AnRpcüohe 1-11, characterized in that the bioreactors are connected in series. 0300SO / OS74