JPS5835759B2 - How to treat organic waste - Google Patents

Description

[Detailed description of the invention] The present invention relates to a method for treating organic waste.

More particularly, the present invention relates to a method for treating biodegradable organic waste in an aqueous medium.

Organic wastes are treated by various industrial and agricultural methods.

Among these treatment methods, for example, methods of burying organic waste, using it freshly buried, or dumping it into the sea are not preferred because they have a negative impact on the environment.

On the other hand, various methods are being used to convert organic waste into energy sources and useful products, such as biological aerobic fermentation, biological anaerobic fermentation, thermophilic aerobic digestion, Examples include cracking distillation (including hydrocarbonization and pyrolysis), incineration, etc.

This method was introduced at the American Academy of Agricultural Engineers (Am.
erican s.

-Ciety of Agricultural En
gineers ) Materials distributed in the northeastern part/! 6NA74107, “Methane Generation from Agricultural Wastes, Concepts and Perspectives on Future Applications” by W. J. Schnill et al.
ation from agricultural tur-al W
astes:Review of Concept a
nd Future A-pp li ca ti o
n), in a report entitled I.

Of this latter group of methods, biological anaerobic fermentation appears to be the most promising and has recently received considerable attention.

As mentioned above, the recent attention paid to biological anaerobic fermentation is probably due, at least in part, to the development of anaerobic streams.

[An example is the International Water Pollution Investigation Association held in Birmingham, England on September 18, 1974.
alAssociation of Water Po
``Jour, Water Pollution Control'' by J. C. Young et al., distributed at the Birmingham Short Course on Biological Treatment Design at 1Lution Research.

ControlFed, ) 141, R160 (196
9) and “Anaerobic Processes” by P. L. Mazzucati.
) and J-C, Giennet et al., Water Pollution Control Journal, 47° 104 (1975).

]An anaerobic stream bed is basically a stream bed filled with pebbles similar to an aerobic flowing stream bed.

However, in an anaerobic bed, the waste stream is dispersed across the bottom of the bed.

The waste stream is forced to rise through the bed of water stones and
The floor is completely submerged in the waste stream.

Anaerobic microorganisms accumulate in the voids between the pebbles and form large active microbial populations.

Generally, the effluent does not contain microbial solids.

(See R160 of the report by J.C. Young et al. above.

) However, anaerobic f-beds as described above are most suitable for the treatment of water-soluble organic wastes.

(See R160 and R171 of the report by J.C. Young et al., supra.

) Furthermore, the chemical oxygen demand (COD) of the waste being treated
), the waste must remain in the bed for a very long time.

That is, the COD of the waste stream is between 36.7 and 93.4.
4-5%, depending on its COD.
A residence time of ~7.2 hours was required.

(See R167 of the report by Young et al. above.

) Furthermore, results such as those described above were achieved for an optimized synthetic waste whose carbon, nitrogen and phosphorus contents were balanced and whose pH value was carefully adjusted.

Therefore, there is a strong need for a waste treatment method that allows for the presence of solids in the waste stream and that allows the actual waste to be disposed of more quickly.

According to the present invention, a method for treating biodegradable organic waste in an aqueous medium comprising sequentially passing the organic waste-containing aqueous medium through a first microorganism immobilization reactor and a second microorganism immobilization reactor, The first reactor is a hydrolytic redox reactor comprising a porous inorganic support suitable for the accumulation of a microbial population, and the second reactor comprises a porous inorganic support suitable for the accumulation of a microbial population. A method is provided, characterized in that the anaerobic reactor comprises a body.

Further, according to the present invention, there is provided an apparatus for treating biodegradable organic waste in an aqueous medium comprising a first microorganism immobilization reactor and a second microorganism immobilization reactor connected to the first microorganism immobilization reactor. , the first reactor is a hydrolysis redox reactor comprising a porous inorganic support suitable for the accumulation of a microbial population, and the second reactor comprises a porous inorganic support suitable for the accumulation of a microbial population. An apparatus is provided that is an anaerobic reactor that includes a support.

The term "biodegradable" as used herein simply means that at least a portion of the organic waste being treated can be degraded by microorganisms.

As a practical matter, usually at least about 50% of organic waste
% by weight is biodegradable.

However, it is necessary to utilize waste materials with a considerably lower content of biodegradable organic substances in the method of the invention;
Or even better.

Therefore, if the organic waste or the aqueous medium containing the organic waste is substantially free of compounds that are toxic to the microorganisms present in any reactor, it may contain non-biodegradable organic or inorganic substances. May contain substances.

Generally the nature of the aqueous medium is not critical.

In most cases, water will constitute at least about 50% by weight of the aqueous medium.

Preferably, water constitutes about 80 to about 98% by weight of the aqueous medium.

In most cases, the waste stream treated by the method of the invention does not require any pretreatment, but in some cases the waste stream may be diluted with water or treated within the apparatus of the invention. Separating from the waste stream excess or extremely coarse solids that would interfere with the operation of the pumping equipment necessary to pass the aqueous medium through the waste stream, such as potassium carbonate, sodium hydroxide, triethylamine, etc. The pH of the aqueous medium is adjusted by the addition of an inorganic or organic base.
It may be necessary or desirable to raise the value.

Also, solid organic waste or organic waste containing almost no water may be diluted as required.

The term "reactor" as used herein means "biochemical reactor" and thus means that the chemical transformations that occur within the reactor are accomplished by microorganisms.

The term "microorganism immobilization reactor" is used to refer to microorganisms in an immobilized state.

As mentioned above, the first and second reactors contain porous inorganic supports suitable for the accumulation of microbial populations.

Conveniently, but not necessarily, the inorganic supports in the two reactors are of the same type.

The inorganic support within each reactor is preferably a porous, high surface area inorganic support suitable for accumulating a large surface area microbial population within a relatively small volume.

More preferably, at least 70% of the pores of the inorganic support have a diameter that is at least as large as the smallest diameter of the microorganisms present in the reactor, but less than five times the largest diameter.

Furthermore, the average diameter of the pores of the inorganic support is about 0.8 to about 2.
Most preferably it is within the range of 20μ.

As used herein, the expression "inorganic support having a large surface area" means an inorganic support having a surface area greater than about 0.01 m' per 11 cm.

Generally, surface area is determined by inert gas adsorption method or B.

Measured by the E,T method.

[For example, Academic Breath Co., Ltd.
Press, Inc., New York) 196
“Adsorption, Surface Area and Porosity” co-authored by S. W. Singh, published in 2007 by S. J. Bretsubu Oyohi.
ion, 5surface Area, and Po
See ro-sityll.

] On the other hand, the pore size is generally determined by the mercury permeation method (mercury 1
nstrusion porosimetry).

[An example is ASTM Publication No. 236, February 1959, N
, M. Winslow and J. J. Shapiro, “
Pore size distribution measuring device by mercury penetration (An Instru
ment for the Measurement
ofPore-8ize Distribution
by Mercury Penetration, )J
checking ...

In general, the inorganic support may be either a siliceous metal oxide or a non-siliceous metal oxide, and may be either amorphous or crystalline.

Examples of siliceous materials include glass, silica, halloysite,
Examples include kaolinite, kinestone, wollastonite, and bentonite.

Examples of non-siliceous metal oxides include alumina, spinel, apatite, nickel oxide, titanium oxide, and the like.

Further, the inorganic support may be made of a mixture of a siliceous material and a non-siliceous material, such as alumina quartzite.

Particularly preferred are calcinite and clay (i.e., halloysite and/or kaolinite) materials, such as those used in the examples described below.

For more information on inorganic supports, see U.S. Patent No. See No. 4.153,510.

As mentioned above, the inorganic support within each reactor provides a site for the accumulation of microorganisms.

The porous nature of the support not only allows for a relatively large accumulation of microbial populations per unit volume of the reactor, but also serves to retain the microorganisms within the reactor.

"Microorganism" (and its derivatives) as used herein
The term is intended to include all microbial valves that decompose organic matter, for example those that utilize organic matter as nutrients.

The term also refers to one of one or more other microorganisms.
It also includes microorganisms that utilize one or more metabolites as nutrients.

Therefore, examples of "microorganisms" include algae, bacteria, mold, yeast, and the like.

Preferred microorganisms are bacteria, molds, and yeasts, with bacteria being most preferred.

Generally, the nature of the microorganisms present within each reactor is not critical.

It is sufficient that the microbial population within each reactor is selected to produce the desired result.

Therefore, the microbial population may consist of a single type of microorganism or multiple types of microorganisms.

Furthermore, the type of microorganism may or may not be confirmed.

Furthermore, if the main functions of the first and second reactors are consistent with their respective reactor designations of hydrolytic redox reactor and anaerobic reactor, the microbial population within each reactor is strictly It need not be aerobic or anaerobic.

The main function of the reactor here means that at least 50% of the microbial population in each reactor has a function consistent with the name of the reactor.

In other words, the boundary line or boundary area between the hydrolytic redox function and the anaerobic function is not critical and does not always need to be between the two reactors.

In practice, such boundary line or boundary area may vary from the midpoint of the first reactor to the midpoint of the second reactor, and may vary depending on the amount of oxygen dissolved in the waste stream. It can be controlled to some extent by adjusting the amount.

However, it is usually not necessary to change the amount of oxygen naturally dissolved in the waste stream.

As used herein, the term "hydrolytic redox" refers to the function of the first reactor to break down the macromolecules present into smaller units, such as monomers and oligomers, by hydrolysis and oxidation-reduction reactions. do.

In performing its function, the first reactor also reduces dissolved oxygen in the aqueous medium.

It is therefore clear that the first reactor is not an aerobic reactor as the term "aerobic" is used in the prior art.

The aqueous medium is not continuously aerated or even saturated with air or oxygen.

However, at least some redox occurs aerobically as residual oxygen in the medium is reduced.

Examples of microorganisms that can be used in hydrolytic redox reactors include Pseudomonas fluorescens (Pseud
omonas fluorescens))
Completely aerobic bacteria such as Escherichia cter calco-acticus and Escherichia coli
coli), Bacillus subtilis (Bacillus 5)
Streptococcus faecalis), Streptococcus faecalis
, Staphylococcus aureus
aureus ) ) Salmonella typhimurium (SaI-mon
ella typhimurium), Klebsiella pneumoniae
iae)) Enterobacter cloker (Entero)
bacter cloacae), facultative anaerobic bacteria such as Proteus vulgaris, Clostridium butyricum (Clo
Stridium butyricum), Bacteroides frazi
lis), Fusobacterium necrofluoran (Fu
sobacterium necrophorum),
Leptotrichia
buccalis), Peironella pavula (ve-i
llonella parvula), Methanobacterium formicicum (Methanobacterium
m formicicum), Metanokotsu Chikara Sumazei (
Methanococcus maze i))
Methanosarcina barkeri (Methanosarcin)
a bar-keri), Peptococcus suanelobius (Pept.

coccus anaerobius), Sarcina ventriculi
), anaerobic bacteria such as trichodermavilide (T
molds such as richoderma viride, Aspirgillus niger, and Sacchar cerevisiae.
O-myces cerevisiae), Saccharomyces ellipsoide (S accharomyces
Yeasts such as S. ellipsoideus) can be mentioned.

Obviously, the hydrolytic redox reactor must not contain only completely aerobic or completely anaerobic microorganisms.

Examples of microorganisms that can be used in anaerobic reactors include facultative anaerobic bacteria, anaerobic bacteria, and yeast, as described above.

Although the presence of fully aerobic microorganisms is generally harmless, it goes without saying that an anaerobic reactor must not contain only fully aerobic microorganisms.

As mentioned above, the microorganisms used in each reactor are selected based on the desired results.

If no specific product is required, the selection of microorganism is based on operational parameters such as temperature, flow rate, waste conversion efficiency, microbial effectiveness, microbial stability, and the like.

On the other hand, if a particular product is desired, the microorganism is generally selected to maximize the product obtained.

Some suitable microbial combinations for producing a given product are illustrated below.

Generally, microorganisms are introduced into each reactor according to conventional methods.

For example, the reactor may be seeded with the desired microorganisms by circulating an aqueous suspension of the microorganisms through the reactor, or the desired microorganisms may be added to the waste stream at an appropriate location.

If the waste stream already contains the appropriate types of microorganisms, passing the waste stream through the two reactors will form the required microbial population in each reactor.

Of course, the reactor may be assembled using an inorganic support on which microorganisms are immobilized.

It will be clear to those skilled in the art that the geometry of the two reactors is not critical to the method or apparatus of the invention.

Therefore, the two reactors may have any shape as long as it does not contradict the idea of the invention.

Typically, conventional cylindrical or tubular flow-type reactors are used, such as those described in the Examples below.

Thus, each reactor generally consists of a cylinder or tube open at both ends, containing an inorganic support.

Generally, such cylinders or tubes are made of a suitable material that is impermeable to gases and liquids.

Suitable materials include glass, stainless steel, glass coated steel, polytetrafluoroethylene, and the like.

Each reactor may be provided with a jacket if necessary.

If a jacket is provided, it is made of conventional materials as described above for the reactor.

If gaseous products are to be stored or handled, the geometry of the second reactor must be designed accordingly.

However, the requirements for such a design will be readily apparent to those skilled in the art.

Each reactor is provided with one or more channels for passage of fluids.

When a plurality of channels are provided, each channel may be independent or may be connected.

The aqueous medium may flow within the channel or around the channel.

Therefore, the inorganic support may be provided within the flow path or may be arranged around the flow path.

For example, in the cylindrical or tubular reactors mentioned above, the inorganic support may be provided within the cylinder or tube;
or a jacket is provided around the cylinder or tube,
An inorganic support may be placed between the jacket and the cylinder or tube.

Thus, the aqueous medium may pass inside or follow around the cylinder or tube.

Of course, removal of gaseous products can be readily accomplished by a variety of known methods.

Generally, gaseous products are withdrawn from a second reactor.

That is, the gas space of the second reactor is connected to the gas sampling means.

In this case, the gas space of the second reactor is connected to the gas sampling means via means for keeping the pressure of the gas sampling means lower than the pressure of the gas space.

Although the processing temperature is only a concern for the survival of the microorganisms present in each reactor, in practice the process of the present invention is carried out at temperatures of about 10 to about 60°C.

Under normal circumstances, it is preferred to maintain the first reactor at an elevated temperature, ie, above ambient temperature.

The preferred temperature range for the first reactor under normal circumstances is about 30 to about 40°C.

As mentioned above, the waste stream treated by the method of the invention can often be used without pre-treatment.

Whether pretreatment is necessary depends primarily on the desired result.

For example, the examples described below describe the treatment of sewage or other waste to obtain an effluent with significantly lower chemical oxygen demand and methane as the main product.

Since the methane thus produced can be used as a fuel, it is desirable to minimize the production of non-fuel gaseous by-products such as carbon dioxide.

However, in order to maintain an acceptable amount of carbon dioxide in the methane, it is necessary to adjust the pH of the sewage to about 8 or higher.

This pH adjustment primarily serves to dissolve carbon dioxide produced by microorganisms into the effluent.

The invention will now be explained in more detail by the following examples illustrating the treatment of sewage.

In the following examples, temperatures are in degrees Celsius ('C) unless otherwise specified.

The method used in the example will be explained with reference to the drawings.

Sewage (or other waste) 1 is passed from a container 2 by a pump 3 into which a rubber tube 5 is connected in a gas-tight manner.
pumped through.

Sewage discharged from the pump 3 is introduced into the hydrolysis redox reactor 4 via a rubber tube 7 into which a pressure gauge 6 is inserted.

This rubber tube 7 connects the pump 3, the pressure gauge 6 and the hydrolysis redox reactor 4 in an airtight manner.

The hydrolysis redox reactor 4 has a glass jacket 9,
It consists of a glass inner cylinder 8 hermetically sealed within this glass jacket 9.

Glass inner tube 8 contains an inorganic support 10 suitable for the accumulation of microbial populations, such as the inorganic support described in U.S. Pat. No. 4,153,510.

The glass jacket 9 is airtightly connected to a constant temperature bath 12 via a rubber tube 11.

The sewage (or other waste) that has passed through the hydrolysis redox reactor 4 is sent to the anaerobic reactor 13 via rubber tube 14.

This rubber tube 14 connects the hydrolysis redox reactor 4 and the anaerobic reactor 13 in an airtight manner.

The anaerobic reactor 13 consists of a glass jacket 15 having an outlet 16 and an inorganic support 10 in the glass jacket 15.
is partially filled, and both ends of the glass jacket 15 are sealed.

The outlet 16 of the glass jacket 15 is connected to a pump 18 via a rubber tube 17.

This pump 18 is a gas space 1 inside the glass jacket 15.
Gas (methane) is extracted from 9.

The extracted gas is collected by a suitable method such as overwater displacement in an inverted vessel (not shown).

A liquid level detection means 20 is attached to the glass jacket 15 of the anaerobic reactor 13.

This liquid level detection means 20 is electrically connected to a liquid level controller 21.

The liquid level controller 21 is electrically connected to the pump 18.

The effluent 22 is sent to a container 25 via a rubber tube 23.

One end of the rubber tube 23 is hermetically connected to the anaerobic reactor 13, and a check valve 24 is connected to the other end.
is installed.

Example 1 Fluid Metering Co., Ltd. (Fluid
Pump RPIG manufactured by Metering, Inc.
6C8C was used.

This pump was connected to the hydrolysis redox reactor 4 with a 14 inch length of rubber tubing.

One end of a 20 inch length of rubber tubing was attached to the inlet of the pump and the other end was placed into a flask containing sewage.

A pressure gauge was inserted into the rubber tube connecting the pump 3 and the hydrolysis redox reactor 4.

As the hydrolysis redox reactor 4, Pharmacia Fine Chemical Co., Ltd.
-micals, Uppsala, Sweden A 16/20 column was used in a Pharmacia equipped with a heavy water jacket.

The water jacket was connected to a constant temperature bath. The column has an average pore size of 3μ and a pore size distribution of 2 to 9μ.
It was filled with 4.5f.

As an anaerobic reactor, a 250 x 15 M Love-Frest column with a jacket of approximately 125 M was used as an anaerobic reactor.
Lab-Crest column) from which the inner cylinder was removed was used.

Therefore, the anaerobic reactor consists of the jacket, and in this anaerobic reactor, the remaining ends of the inner cylinder serve to seal both ends of the reactor.

This anaerobic reactor was filled with the above-mentioned kinezoite support 51P, and the reactor was installed in a substantially horizontal position.

The two reactors were connected with approximately 4 inch rubber tubing.

The total fluid capacity of the pump, rubber tubing and both reactors was 120d.

A short Tygon tube was attached to one end of the anaerobic reactor (jacket) and the tube was closed with a clamp.

In addition, a thick-walled tie-bon tube was attached to the other mouth of the anaerobic reactor, and a
Chler Instruments, Inc.
Buchler Polystaltic Pump manufactured by Fort Lee, N.J.
tic pump).

Seeding of the above-mentioned processing apparatus was carried out as follows.

The rubber tube from the pressure gauge was removed from the inlet of the hydrolysis redox reactor.

A rubber tube from an anaerobic reactor of a similar device in operation was attached to this inlet.

The two devices were operated in conjunction for 13 days using sewage as the feed liquid.

The gases generated in the anaerobic reactor were collected by displacement over water in a graduated cylinder placed upside down in a shallow vessel filled with water.

Gas evolution rates were measured and the collected gases were analyzed by mass spectrometry at least daily.

Furthermore, the chemical oxygen demand (COD) of the sewage used as feed liquid and the C of the effluent leaving the anaerobic reactor
OD was measured periodically by the well-known standard dichromate oxidation colorimetric method.

Table 1 shows the performance of the processing equipment during this seeding period.

After seeding as described above, the processor was removed from a similar processor in operation and the rubber tube from the pressure gauge was reattached to the inlet of the hydrolysis redox reactor.

After that, pH 8.6 to 8.
The treatment equipment was operated using sewage water adjusted to 9.9 as the feed liquid.

The data obtained are shown in Tables 2 and 3.

Table 2 shows the operating parameters and gas composition, and Table 3 shows the performance of the treatment equipment and changes in carbon content.

Example 2 Pore size distribution is 0.4 to 6μ, and average pore size is 4.5μ
, the pore volume is 0.4 cc/f, and the porosity is 51.5%.
ery, Rambervillers, Franc
e) Duralite Rouge (Duralite Rouge)
Rouge) was used as the support, and this support was added to the hydrolytic redox reactor and the anaerobic reactor, respectively.
A processing apparatus was constructed in the same manner as in Example 1, except that 2g and 52.51 were used.

The treatment equipment was seeded in the same manner as in Example 1, except that the temperature of the constant temperature bath was adjusted to 31° C. and the two connected treatment equipment were operated for about 6 days.

Additionally, one psi check valve was inserted at the end of the effluent rubber tubing from the anaerobic reactor.

The performance of the processing equipment was monitored over the next 33 days, but satisfactory performance was not observed until the 40th day of operation (including 6 days of operation with two processing equipment connected). .

20 days after the start of operation: 1 psi check valve on 3 plates
Replaced with 1 psi check valve.

Data obtained on the 40th day after the start of operation are shown in Tables 4 and 5.

Table 4 shows the operating parameters and gas composition, and Table 5 shows the performance of the treatment equipment and changes in carbon content.

Example 3 F, Duralite No. 1- manufactured by Garley Co., Ltd., has a pore size distribution of 0.8 to 30 μ, an average pore size of 6 μ, and a porosity of 34.1%.
re) was used as a support, and this support was injected into a hydrolytic redox reactor and an anaerobic reactor at 20S', respectively.
A processing apparatus was constructed in the same manner as in Example 1 except that 50S' was filled.

Seeding of the processing equipment was carried out in the same manner as in Example 2 for 10 days.

No appreciable reduction in COD was observed until day 34 of operation.

Accordingly, Tables 6 and 7 show data obtained on a 34-day withdrawal.

Table 6 shows the operating parameters and gas composition, and Table 7 shows the performance of the treatment equipment and changes in carbon content.

Example 4 Johns-Manville Co., Ltd., with a pore size distribution of 2 to 15 μ, an average pore size of 9 μ, a pore volume of 1.0 CC/S′, and a porosity of 68%. Ma
nville Corp, , Denver, Co.
John-s-Manville fireproof insulation brick JM-23 (John-s-Manville I
nsulating Firebrick JM-2
A treatment apparatus was constructed in the same manner as in Example 1, except that 10f and 15f of this support were used in the hydrolysis redox reactor and anaerobic reactor, respectively.

Seeding of the processing equipment was carried out in the same manner as in Example 2 over a period of 7 days.

Satisfactory performance was observed on the 29th day after the start of operation.
Periodic leakage became a problem when I self-administered it on the 37th.

The data obtained on the 29th day of the test are shown in Tables 8 and 9.

Table 8 shows the operating parameters and gas composition, and Table 9 shows the performance of the treatment equipment and changes in carbon content.

[Brief explanation of the drawing]

The drawing is a schematic illustration of an example of an apparatus for carrying out the method of the invention. 1... Sewage (waste), 2... Container,
3...Pump, 4...Hydrolysis redox reactor, 6...Pressure gauge, 8...Glass inner cylinder, 9... Glass jacket, 10...
... Support body, 12 ... Constant temperature bath, 13 ...
... Anaerobic reactor, 15 ... Glass jacket, 16 ... Anaerobic reactor outlet, 18 ...
...pump, 19...gas space, 20...
...Liquid level detection means, 21...Liquid level controller, 2
2...Flowing liquid, 24...Check valve, 25...Receiver is container, 5, 7, 11°14.
17,23...Rubber tube.

Claims (1)

[Scope of Claims] 1. A method for treating biodegradable organic waste in an aqueous medium, which comprises sequentially passing the organic waste-containing aqueous medium through a first microorganism immobilization reactor and a second microorganism immobilization reactor. , the first microorganism immobilization reactor is a hydrolysis redox reactor comprising a porous inorganic support suitable for the accumulation of a microbial population, and the second microorganism immobilization reactor is a porous inorganic support suitable for the accumulation of a microbial population. A treatment method characterized in that it is an anaerobic reactor containing a quality inorganic support. 2. The treatment method according to claim 1, wherein the anaerobic reactor includes gas removal means. 3. The treatment method according to claim 1, characterized in that the hydrolysis redox reactor is maintained at a temperature of 10 to 60°C. 4. The treatment method according to claim 3, characterized in that the hydrolysis redox reactor is maintained at a temperature of 30 to 40°C. 5. The inorganic support of the hydrolysis redox reactor and/or the anaerobic reactor is a porous, high surface area inorganic support suitable for accumulating a large surface area microbial population within a relatively small volume. A processing method according to claim 1, characterized in that: 6 At least 70% of the pores of the inorganic support are at least as large as the minimum diameter of the microorganisms present in the hydrolytic redox reactor and/or anaerobic reactor, but the maximum diameter of the microorganisms is The treatment method according to claim 5, characterized in that the treatment method has a diameter smaller than 5 times the diameter of the treatment method. 7. The treatment method according to claim 5, wherein the average pore diameter of the inorganic support is within the range of 0.8 to 220μ. 8. The treatment method according to claim 7, wherein the inorganic support is made of a calcinite material. 9. Process according to claim 8, characterized in that the trichlorite inorganic support has a pore size distribution of 2 to 9 microns and an average pore size of 4.5 microns. 10. The treatment method according to claim 7, wherein the inorganic support is made of halloysite material, kaolinite material, or both. 11. Process according to claim 10, characterized in that the inorganic support has a pore size distribution of 0.4 to 6μ and an average pore size of 4.5μ. 12. The treatment method according to claim 10, wherein the inorganic support has a pore size distribution of 0.8 to 30μ and an average pore diameter of 6μ. 13 The inorganic support has a pore size distribution of 2 to 15μ and 9
11. The treatment method according to claim 10, wherein the treatment method has an average pore diameter of μ. 14. The treatment method according to any one of claims 1 to 13, wherein the main product of the anaerobic reactor is ethanol. 15. The treatment method according to any one of claims 1 to 14, characterized in that the hydrolysis redox reactor and the anaerobic reactor are connected in series.