WO1996009986A1

WO1996009986A1 - Method and apparatus for treating a liquid medium containing organic waste

Info

Publication number: WO1996009986A1
Application number: PCT/FR1995/001246
Authority: WO
Inventors: Jean Paul Raes; Sylvain Danda; Bernard Castelas; Yvette Pescher; François RABATEL; José MORALES; Jean Bonfill
Original assignee: Rhone-Poulenc Chimie
Priority date: 1994-09-28
Filing date: 1995-09-27
Publication date: 1996-04-04
Also published as: FR2724922A1; AU3570295A; FR2724922B1

Abstract

A method for treating a liquid medium containing organic waste by carrying out one or more liquid/solid separation steps (A) and optionally one or more physico-chemical treatment steps (B, C) on the medium to provide a medium containing no more than 20 g/l and preferably no more than 5 g/l of solids in suspension, and carrying out an ultra- or microfiltration step (E) on the resulting liquid medium to give a retentate and an ultra- or microfiltrate. An apparatus for treating a liquid medium containing organic waste, particularly pig manure, is also disclosed.

Description

Method and installation for treating a liquid medium containing organic waste ".

The present invention relates to a method and an installation for treating a liquid medium containing organic waste. It also relates to the application of said method to the treatment of organic excrement and in particular of animal manure, in particular pig manure.

It also relates to the application of this process to the treatment of other effluents such as effluents from the food industry, in particular the production of olive oil and wine.

The treatment of organic waste in particular, with a view to its elimination and / or recovery is a need which is increasingly felt in today's industrial and agricultural world.

Thus, the high production of waste water of agricultural origin, in particular of animal slurry, poses increasingly important problems for agriculture and also for the protection of the natural environment, in particular of watercourses and groundwater. Increasingly stringent regulations are being put in place to avoid the very negative effects of pollution of the natural environment due to the various animal manures.

A number of treatment methods have been proposed. It is known, for example, to treat fermentable and foul-smelling waste with oxidizing agents. It has also already been proposed to sterilize the slushes of the cities using gases containing nitrous gases. Likewise, the possibility of destroying putrid compounds contained in household waste by means of gases containing nitrogen oxides has been mentioned in the past. Nevertheless these process of purification of medium (or effluent) containing organic waste do not give entirely satisfactory results from a technical and even economic point of view. This is particularly the case for the treatment of animal manure.

These usually involve one or more of the following steps:

1 - liquid-solid separation such as centrifugation, decantation, sieving, pressing, concen¬ tration by natural, forced evaporation, or with mechanical vapor compression (CMV) ... 2 - physico-chemical treatment: coagula¬ tion-flocculation, chemical or electrochemical oxidation. 3 - biological treatment: activated sludge, nitrification-denitrification, natural or reinforced lagooning by culture of algae, hyacinths ... We can also mention a process of destruction by combustion as well as the drying of whole manure by evaporation of water it contains which has the disadvantage of causing air pollution and a gene for smell. The known methods for purifying the medium (or effluent) containing organic waste have the drawback of not always treating the problem of pollution as a whole. Those who manage to do so, particularly in the case of pig manure, require large-scale installations which require transporting the manure to a collective treatment center. In addition to significant congestion on the roads, the contagion factor from one farm to another requires sanitary maintenance of the means of transport. The present invention proposes to solve the above-mentioned drawbacks. To this end, the present invention provides a method and a compact installation operating according to a method for purifying a medium (or effluent) containing organic waste, in which said medium is subjected to a combination of particular chemical, physical or physico-chemical treatments, all the organic waste contained in this medium being treated and, preferably, no non-recovered waste remaining at the end of the process, the implementation of which is simple and economical. In addition, the rejection into the natural environment (watercourse, irrigation ...) or the recycling of the aqueous part of the effluents treated according to the present invention becomes possible because it is advantageously odorless, limpid, sterile and very poor. in BOD (biological oxygen demand) and COD (chemical oxygen demand).

Finally, the present invention makes it possible to obtain, especially in the case of the treatment of animal manure (in particular pig manure), directly spreadable sludge, that is to say directly usable as an agricultural amendment without that it is generally necessary to add fertilizer additives. The subject of the invention is therefore a method of treating a liquid medium containing organic waste, characterized by the following successive steps:

- the medium is subjected to one or more stages of liquid / solid separation and optionally one or more stages of physicochemical treatments so as to obtain a medium containing not more than 20 g / 1, preferably 5 g / 1 of materials suspended solids,

- The medium thus obtained is subjected to an ultra- or micro-filtration step, whereby a retentate and an ultra- or n-o-filtrate are obtained.

The ultrafiltrate or micro-filtration operation is a known technique which: part of membrane separation techniques whose driving force for transfer is a pressure gradient. It is carried out here using any adequate ultrafiltration or microfiltration device.

The ultrafiltration or microfiltration employed in the present invention can be frontal or, preferably tangential. In the latter case, the operating principle generally consists in circulating the effluent to be treated under pressure along a membrane permeable to the solvent but impermeable to the solutes which it is desired to retain. The membrane used to carry out the ultrafiltration operation in the process according to the invention can be organic or inorganic.

It can be homogeneous, asymmetrical or composite. A membrane is said to be asymmetrical when the permselective layer represents only a very thin thickness of the membrane; by contrast, the homogeneous membrane as a whole constitutes the permselective layer; a special case of an asymmetric membrane is the composite membrane obtained by depositing the permselective layer on a pre-existing support.

The configuration of the membrane used is for example multichannel, tubular, spiral or preferably planar.

Its cutoff threshold is generally between 0.001 and 0.5 micrometer.

It is possible to use as a membrane in the context of the invention in particular a mineral zirconia membrane deposited on an alumina support, made of carbon stainless steel (for example with a cutoff threshold of 0.14 μm). It is also possible to use an organic membrane based on polysulfone, fluorinated polyvinylidene or preferably based on acrylonitrile copolymers (for example, cutoff threshold 40 KD).

It is also possible to use a mineral membrane on a monolithic support as described in the application. European patent EP-A-0 585 152.

At the end of the ultra- or micro-filtration operation, a retentate (or concentrate) and an ultra- or microfiltrate (or permeate) are obtained. The inventors have found that the permeate obtained at the end of the ultrafiltration or microfiltration step is relatively odorless, not very colored and also sterile (disinfected), clear and relatively low in BOD and COD. Consequently, this permeate can not only be sent to water purification stations but also directly discharged into the natural environment for irrigation of crops, for example.

The retentate (or concentrate) obtained at the end of the ultrafiltration or microfiltration stage is preferably recycled to the stage or stages of liquid / solid separation.

The effluent from the ultra- or microfiltration step can also advantageously be subjected to a reverse osmosis operation.

We then obtain a second retentate (had concentrate) and a second filtrate (or permeate).

The reverse osmosis operation is a technique well known to those skilled in the art and is part of the membrane separation techniques whose driving force for transfer is a pressure gradient.

The reverse osmosis employed in the present invention is preferably tangential. The operating principle consists in circulating the effluent to be treated at a pressure higher than its osmotic pressure along a membrane permeable to water but impermeable to solutes, organic matter in solution and to salts.

The efficiency of the separation can then be adjusted by the choice of membranes and pressures in order to produce a final permeate of quality adapted to its post-treatment use.

The configuration of the membrane can be tubular, discoid (disc-shaped), planar and preferably spiral. The membrane used to carry out the reverse osmosis operation in the process according to the invention is preferably organic, it can be supported by an organic or inorganic material. It is generally of the cellulose acetate type and preferably a polysulfone-polyamide mixture.

The filtrate from the reverse osmosis step is a colorless, odorless liquid, the BOD / COD content of which allows discharge into the natural environment according to European standards. According to the invention, the step (s) of liquid / solid separation can (can) comprise at least one filtration step the aim of which is to lower the content of solid matter suspended in the medium to a lower level 20 g / l, advantageously less than 5 g / l, optionally after subsequent treatment by physicochemical processes, so that the medium thus obtained can then be treated by ultra- or microfiltration.

This filtration step can be carried out using a rotary drum comprising an endless screw making it possible to evacuate the solids in proportional quantity at the variable speed of rotation as a function of the desired flow rate. The solid residue from this step can be removed to a storage location. The sludge thus obtained can be used for silage or shoveling.

Before the filtration step, it is also possible advantageously to carry out a step of coarse liquid / solid separation making it possible to separate from the medium. relatively large solid particles. Its purpose is to lower the content of suspended solids to a value below 20% (by weight).

This operation can be carried out with a sieve having a mesh size of between 0.1 and 10 mm. The solids obtained at the end of this stage are stored and used, after drying, for example for silage and shoveling.

The method according to the invention can also comprise a physico-chemical treatment of coagulation, and / or flocculation, advantageously at the end of the previous step of coarse liquid / solid separation, and / or just before the filtration step.

Thus, the effluent from the sieving step can be treated using at least one coagulating agent, preferably mineral. Any type of coagulating agent, preferably mineral can be used. Preferably, the coagulating agent used is an iron or aluminum salt. This iron salt can correspond to the following formula (1):

Fe ₂ Cl, (S0 ₄ ) _y (1)

in which 0≤x≤6, 0≤y <3 and x + 2y≈6. Likewise, this aluminum salt can correspond to the following formula (2):

Al ₂ (0H) .Cl _b (S0 ₄ ) _c (2)

in which 0≤a <6, 0≤b.s6, 0 <c <3 and a + b + 2c ”6.

The coagulating agent can in particular be chosen from the group formed by ferrous chloride, ferric chloride, ferrous sulfate, ferric sulfate, ferric chlorosulfate, aluminum sulfates, basic aluminum chlorosulfates. We can use a mixture of coagulating agents. The amount of coagu¬ lant agent used is generally between 0.1 to 80 liters per cubic meter, preferably between 10 and 50 liters / m ³ . The coagulation step is preferably carried out with stirring.

The coagulating agent must usually be chosen in such a way that its use does not generate decarbonation due to the destruction of the carbonates and hydrogen carbonates possibly present in the effluent to be treated. It is generally sufficient for the pH value of the reaction medium not to drop below that of the destabilization pH of the carbonates and hydrogen carbonates. The coagulating agent can be used in the presence also of at least one cationic or neutral polyelectrolyte. The polyelectrolytes which can be used in the present invention are in particular:

- neutral polyamines and quaternary polyamines; more specifically, mention may be made of polyalkylamines and polyhydroxyalkyla ines, neutral or quaternary; the following homopolymers are particularly suitable:. polyethyleneamine, poly-hydroxy-2-propyl-1N-methylammonium, poly-hydroxy-2-propyl-1,1-N-dimethylammonium, polyvinyl-2-imidazolinium hydrochloride, diallyl-dimethyl polychloride -am onium; mention may also be made of the copolymer formed by acrylamide and diallyl-dimethylammonium chloride;

. polyaminoacrylates and polyamino ethacrylates, and more precisely polydialkylaminoalkylacrylates and polydialkylaminoalkylmethacrylates; by way of example, the neutral or quaternary poly-N, N-dimethylaminoethylmethacrylate is suitable, whether under the form of the homopolymer or of a copolymer with acrylamide;

. polyaminoacrylamides and polyaminomethacrylamides, and more precisely polydialkylaminoalkyl-acrylamides or -methacrylamides; as examples, mention may be made of poly-N-dimethylaminopropylmethacrylamides poly-N-dimethylaminoethylacrylamides.

A mixture of cationic and / or neutral polyelectrolytes can be used. The amount of cationic and / or neutral polyelectrolytes capable of being used relative to the amount of mineral coagulating agent is advantageously between 0.01 and 5%, in particular between 0.1 and 0.3%. The coagulation step constitutes a step of conditioning the effluent to be treated. In addition, the Applicant has found that this step leads to the precipitation of phosphate-based compounds and those based on phosphorus and generally of protein compounds, and also to a reduction in BOD (biological oxygen demand). and COD (chemical oxygen demand).

The process of the invention can also comprise, after the coagulation step, a flocculation step, preferably using at least one anlonic polyé¬ electrolyte.

Preferably (but not limiting), the anelonic type polyelectrolyte capable of being used is an anionic polyacrylamide, a polyacrylate, a polymethacrylate, a polycarboxylate, a polysaccharide (for example xanthan gum, guar gum, alginate) or chitosan.

A mixture of anionic type polyelectrolytes can be used. The amount of polyelectrolytes used in this step is generally between 1 and 100 grams, preferably between 2 and 20 grams, expressed by weight of dry polyelectrolyte, per m ³ of organic waste (present in the initial medium to be treated). The inventors have found that thanks to the prior elimination of colloids, in particular fine hydrophilic colloids, the effluent obtained at the end of the flocculation step was essentially formed from a directly dehydratable sludge, for example during the 'subsequent filtration step.

The method according to the invention does not generally comprise a treatment step using an oxidizing agent before the ultra- or micro-filtration step, as described in FR-A -2,715,590. However, it may include such a step before the ultra- or micro-filtration step in the case where it comprises a step of coarse liquid / solid separation, in particular of sieving using a sieve with a mesh size of between 0.1 and 10 mm, and / or a reverse osmosis step of the ultra- or micro-filtrate.

Preferably (but not limiting), the oxidizing agent used is chosen from the group formed by oxygen, oxygenated derivatives, in particular peroxides (for example hydrogen peroxide, ozone), chlorine, derivatives chlorinated (e.g. chlorine dioxide, sodium hypochlorite, calcium hypochlorite, potassium hypochlorite, sodium chlorite, sodium chlorate, bleach), potassium permanganate.

A mixture of oxidizing agents can be used.

The amount of oxidizing agent used is generally between 0.1 and 50 liters, preferably between 0.5 and 10 liters, per m ³ of organic waste. ques (present in the initial medium to be treated).

Bleach will advantageously be used as an oxidizing agent; the amount of bleach then used is then generally between 0.1 and 5 liters, preferably between 0.5 and 1 liter, per m ³ of organic waste (present in the initial medium to be treated).

The Applicant has found that the treatment carried out during the oxidation step notably allows the oxidation of fine hydrophilic colloids and the elimination of sulfurous compounds, in particular hydrogen sulfide (H ₂ S), possibly present in the medium to be treated.

The method according to the invention can also include a step of treatment with an oxidizing agent after the step of ultra- or micro-filtration and before the reverse osmosis step, in case it includes such a step of reverse osmosis.

In this case, the oxidizing agent is as defined above and preferably oxygen (from the air) or a peroxide.

The purpose of this treatment immediately before the reverse osmosis step is to oxidize the ammonium ions present in the medium to be treated into nitrates, which has the effect of increasing the efficiency of the reverse osmosis membranes.

According to a preferred embodiment, the process of the invention successively comprises the following stages: (A) Treatment of the liquid or effluent medium

(containing organic waste) using a liquid-solid separator, whereby a first filter cake and a filtrate are obtained; the filtrate can be recycled in whole or in part in the feed device, (B) treatment of the filtrate from step (A) using at least one coagulating agent,

(C) treatment of the effluent obtained at the end of step (B) using a flocculating agent, preferably an anionic polyelectrolyte

(D) subjecting the effluent obtained at the end of step (C) to filtration, whereby a second filtration cake and a filtrate are obtained; the filtrate from step (D) can optionally be recycled in whole or in part to step (A), or in the feed device,

(E) submitting the effluent obtained at the end of step (D) to an ultra or microfiltration on a membrane, whereby a retentate and a filtrate are obtained, the retentate preferably being recycled to step ( A), or in the feeding device,

(F) subjecting the effluent from step (E) to a reverse osmosis type treatment, whereby a permeate and a concentrate are obtained, the concentrate preferably being recycled to step (A), or in the feeder.

Advantageously, the process further comprises before the reverse osmosis step a step of treatment with an oxidizing agent, as described above. The invention also relates to an installation, in particular intended for the treatment of a liquid medium containing organic waste, caracté¬ risée in that it comprises:

- Liquid / solid separation means and optionally means for carrying out a physico-chemical treatment capable of providing a liquid medium containing not more than 20 g / 1, preferably 5 g / 1 of suspended solids;

- means of ultra- or micro-filtration. The installation may also include means to achieve reverse osmosis.

The liquid / solid separation means capable of providing a medium containing not more than 20 g / l, preferably 5 g / l of solid matter in suspension, optionally after additional physicochemical treatment advantageously comprise a sieve of dimension of mesh between 0.1 and 10 mm. These means may for example consist of a comb screen, a linear screen or a rotary drum. The installation according to the invention can also comprise means for producing coagulation and / or flocculation of the medium to be treated.

The process and the installation according to the invention will be better understood from the following detailed description for which reference will be made to the appended figures, in which:

- Figure 1 shows the general diagram of an embodiment of an installation for implementing the method according to the invention, - Figure 2 shows, schematically in longitudinal section, the rotary drum of the separation step liquid / solid,

- Figure 3 shows a section along line 3-3 of Figure 2. As shown in Figure 1, the medium to be purified is pumped through a pump 1 from the bottom of a pit 2 to 'to a rotary drum designated as a whole by the reference 3. Referring to Figures 2 and 3, we will describe a preferred embodiment of the rotary drum 3.

This rotary drum 3 comprises an envelope composed of a succession of strips 31 of triangular section and arranged parallel to each other. others and to the longitudinal axis of the envelope. These strips 31 have their apex directed towards the outside of the envelope and are for example made of stainless steel. They provide an interval between 600 and 1200 μm between them.

On the other hand, the rotary drum 3 is internally provided with turns 32 parallel to each other. These turns 32 are integral at their peripheral edge 32a with strips 31 and provide a free space 33 in the longitudinal axis of the drum as shown in FIG. 3. The turns 32 are for example made of stainless steel and have a pitch from 50 to 100 mm.

The strips 31 are interconnected at each of their ends by two flanges, respectively 34 and 35 perpendicular to the longitudinal axis of the drum 3.

The rotary drum 3 is inclined relative to the horizontal axis by an angle between 1 and 45 ^e , advantageously between 10 and 20 °, which is a function of the desired degree of drying of the solids obtained at the end of the step liquid / solid separation.

The rotary drum 3 also comprises a tube 36 for supplying the medium to be purified, disposed in the longitudinal axis and extending over the entire length of said drum.

This tube 36 has, at its upper end 36a, an orifice for supplying the medium to be purified and at its lower end 36b a longitudinal slot 37 for leaving the medium to be purified in the drum 3.

The flange 35 is provided with an orifice 35a for leaving the solids contained in the medium to be purified as will be seen later.

The assembly formed by the strips 31, the turns 32 and the flanges 34 and 35 is driven in rotation by a motor-variator 38 while the tube 36 is fixed.

The rotary drum 3 thus described operates as follows: The medium to be purified is introduced into the tube

36 at its upper end 36a and flows inside said tube to its lower end 36b where it falls into the drum 3 through the slot 37.

The strips 31 and the turns 32 are rotated by the motor-variator 38 so that these turns stir the medium to be purified, so that the liquids fall into the tank 40 through the strips 31 of the lower part of the drum towards the upper part of this drum where they are discharged through the orifice 35a on a conveyor 4.

The rotary drum 3 can be replaced by a comb screen, having a mesh size between 1 and 5 mm or any other similar system consisting for example of a linear sieve having a mesh size preferably between 0.03 and 1 mm.

The liquid / solid separation step (A) is carried out continuously. The treatment capacity of step (A) ensures significant recycling of the permeate between 10 and 100%, advantageously 50 to 85%, this in order to stir the medium to be treated in order to bring down the COD of the medium.

The solids separated in step (A) are conveyed by an automatic device consisting of a drip mat 4, with return of the liquids to step (A), on a storage area 5 where, after subsequent drying, they can be used for silage and shoveling.

The effluent obtained at the end of step (A) is then pumped via the pump 6 to a coagulator 7.

Upstream of the coagulator 7, the coagulant is injected from a reservoir 8 for storing the coagulating agent. The coagulator 7 consists of a tubular reactor (not shown) fitted with axial blades allowing both to ensure a peripheral rotation speed between 0.5 and 7 ms ^"1 , advantageously 0.8 and 5 ms ^{" 1} and a coil 9 in Plymouth piping producing a dead volume allowing a contact time of the medium with the coagulating agent of between 10 s and 15 min, advantageously 30 s and 2 min.

After stage (B), the medium to be treated is conveyed to stage (C) of flocculation. The apparatus 10 used for the flocculation is identical to the coagulator 7 of step (B) except for the speed of rotation of the blades which is lower and is in the range of 0.5 to 3 ms " ¹ , advantageously from 1 to 1.5 ms ^{" 1} and that it does not comprise a coil ensuring a dead volume.

Upstream of the flocculator 10 is injected the flocculant from a reservoir 11 for storing the flocculating agent.

The axes of the coagulator 7 and the flocculator 10 are driven by the same motor.

At the end of step (B) the medium to be treated can be sent directly to step (D) without undergoing step (C).

In step (D), the effluent obtained at the end of step (B) or (C) undergoes a filtration operation. The device used for this purpose consists of a rotary drum 12 of the same type as that described for step A consisting of strips 13 of triangular section and made of stainless steel. But for this drum the interval between the lamellae is between 150 μm and 500 μm. The solids are discharged in an amount proportional to the speed of rotation of the turns which is variable and ranges from 5 to 75 revolutions per minute depending on the desired flow rate. The solid residues are then evacuated to the storage area 5 via a conveyor belt 14 where they are subsequently dried.

The effluent from step (D) is collected in a tank 14 comprising an overflow 15 which returns to the pit 2 and is conveyed to step (E) where it is subjected to ultrafiltration.

The ultrafiltration is tangential and carried out in a manner known per se on an ultrafiltration device 15 comprising an ultrafiltration module 16 equipped with an organic membrane made of acrylonitrile copolymers having a cutoff threshold of 40 KD, as well as in known manner a feed pump 17 and a recirculation pump 18 as well as a recircu¬ lation loop 19. The retentate obtained at the end of step (E) is recycled to step (A).

The effluent from the ultrafiltration stage (E) can be discharged directly into the environment or collected in a tank 20 from which it is conveyed to stage (F) where it is subjected to reverse osmosis.

Until the ultrafiltration module 10 reaches an optimal operating level, the effluent in the tank 20 is recycled to the tank 2 by a pipe 21.

The reverse osmosis device 22 according to the invention comprises, in a known manner, a reverse osmosis membrane of known type, of spiral form consisting of a polysulfone-polyamide mixture deposited on an organic support, as well as a feed pump. 23 and a recirculation loop 24.

Reverse osmosis is of the tangential type.

The effluent obtained at the end of this stage is rejected in the natural state. The process according to the invention is a process which can be carried out continuously.

It can be used directly on the effluent producer site and adapts to all types of flow without prior collection obligation. There remains at the end of the process according to the invention no non-recovered waste, the treatment producing a solid pellet which can be recovered, for example by agricultural spreading, and a liquid which can be recovered for agricultural irrigation or discharged into the natural environment. The method according to the invention can be used to purify the media (or effluents) containing organic excrement, in particular animal manure, in particular of the bovine, poultry, sheep or pig type. It is for example advantageously used for the treatment of pig manure, and this directly on the place of the agricultural exploitation concerned.

The method according to the invention can also be applied to the treatment of effluents from the production of olive oils and to the treatment of waste water from the cleaning of wine tanks.

The advantages of the process according to the invention are in particular:

- The process according to the invention is a physical process whose start-up is immediate and, unlike biological processes, allows it to stop operating when it is desirable;

- The process of the invention can be adapted to all the capacities of the medium to be treated (from a hundred liters / day to several tens of m ³ / day); - it implements membrane techniques allowing total purification; the sequence of successive stages allows an optimized operation, allowing high fluxes on the membranes and a large spacing of the washing phases.

Claims

1. Process for treating a liquid medium containing organic waste, characterized by the following successive stages: - the medium is subjected to one or more stages of liquid / solid separation and possibly one or more stages of physico-chemical treatment so to obtain a medium containing not more than 20 g / l, preferably 5 g / l of suspended solids,

- The liquid medium thus obtained is subjected to an ultra- or micro-filtration step, whereby a retentate and an ultra- or micro-filtrate are obtained.

2. Method according to claim 1, characterized in that the ultra- or micro-filtration consists of a tangential ultra- or micro-filtration.

3. Method according to claim 1 or claim 2, characterized in that the ultra- or micro-filtration is carried out by means of a membrane having a cutoff threshold between 0.001 and 0.5 microns.

4. Method according to any one of claims 1 to 3, characterized in that one rejects the ultra- or micro-filtrate directly in nature.

5. Method according to any one of claims 1 to 4, characterized in that the utra- or micro-filtrate is subjected to a reverse osmosis step.

6. Method according to claim 5, caracté¬ ized in that the reverse osmosis operation is of tangential type.

7. Method according to claim 5 or claim 6, characterized in that the ultra- or micro-filtrate is subjected before the reverse osmosis step to a treatment step using an oxidizing agent.

8. Method according to any one of the preceding claims, characterized in that the (them) liquid / solid separation step (s) comprises (compren¬ nent) at least one filtration step.

9. The method as claimed in claim 8, characterized in that before the filtration step is carried out a step of coarse liquid / solid separation, in particular of sieving using a sieve of mesh size between 0, 1 and 10 mm.

10. Method according to any one of the preceding claims, characterized in that before the ultrafiltration step, a coagulation and / or flocculation operation is also carried out, using a coagulating agent and / or a flocculating agent.

11. The method of claim 10, characterized in that during the coagulation step is added to the coagulating agent a polyelectrolyte of cationic or neutral type.

12. Method according to claim 10, characterized in that the flocculating agent is an anionic polyelec¬ trolyte.

13. Method according to any one of the preceding claims, successively comprising the following steps:

(A) sieving;

(B) coagulation; (C) preferably flocculation using a polyelectrolyte;

(D) filtration;

(E) ultrafiltration; and optionally, (F) reverse osmosis.

14. Method according to any one of the preceding claims, successively comprising the following steps:

(A) sieving; (B) coagulation; (C) preferably flocculation using a polyelectrolyte;

(D) filtration;

(E) ultrafiltration; (Fj) treatment with an oxidizing agent; and

(F ₂ ) reverse osmosis.

15. Installation, in particular intended for the treatment of a liquid medium comprising organic waste, characterized in that it comprises:

means of liquid / solid separation (3.12) and optionally means of carrying out a physico-chemical treatment (7.10) capable of providing a liquid medium containing not more than 20 g / l, preferably 5 g / 1 of suspended solids;

- means of ultra- or micro-filtration (15).

16. Installation according to claim 15, characterized in that the ultrafiltration means (15) comprise a membrane having a cutoff threshold of between 0.001 and 0.5 μm.

17. Installation according to claim 15 or 16, characterized in that the ultrafiltra¬ tion means comprise a zirconia membrane deposited on a carbon or alumina support, a carbon membrane deposited on a support based on carbon fibers or an organic membrane based on polyacrylonitriles or an inorganic membrane deposited on a ceramic support.

18. Installation according to claim 15, characterized in that it further comprises means for carrying out reverse osmosis (22).

19. Installation according to claim 18, characterized in that said means for carrying out reverse osmosis comprise a membrane of cellulose acetate or polysulfone-polyamide type, optionally deposited on an organic or inorganic support.

20. Installation according to claim 19, characterized in that it further comprises filtration means.

21. Installation according to claim 20, characterized in that the filtration means comprise a drum type device (12) with a rotary fabric comprising turns and strips (13) spaced from one another with an interval of between 150 and 500 μm.

22. Installation according to claim 21, characterized in that the drum (12) is inclined at an angle of 1 to 45 degrees / horizontal axis, advantageously from 10 to 20 degrees.

23. Installation according to any one of claims 15 to 22, characterized in that it further comprises means for carrying out a coarse liquid / solid separation (3).

24. Installation according to claim 23, characterized in that said means comprise a drum type device (3) comprising turns (32) integral with strips (31) spaced from each other with an interval between 600 and 1200 μm .

25. Installation according to any one of claims 15 to 24, characterized in that it further comprises coagulation means (7).

26. Installation according to claim 25, characterized in that said coagulation means (7) comprise a tubular reactor provided with axial blades and comprising a dead volume (9) allowing a sufficient contact time to obtain coagulation.

27. Installation according to one of the preceding claims, characterized in that it further comprises flocculation means (10).

28. Installation according to claim 27, characterized in that the flocculation means (10) comprise a second reactor of the same type as the coagulation reactor defined in claim 25, the axial blades of which rotate with a speed lower than that of said coagulation reactor.

29. Installation according to one of the preceding claims, characterized in that it further comprises means for carrying out a treatment using an oxidizing agent.

30. Application of the method according to one of claims 1 to 14, and of the installation according to one of claims 15 to 29 to the treatment of organic manure, in particular of animal manure or to the treatment of effluents from olive oil or wine production.