EP1583602A1 - Procede et systeme de traitement de fumier de porc - Google Patents

Procede et systeme de traitement de fumier de porc

Info

Publication number
EP1583602A1
EP1583602A1 EP00930914A EP00930914A EP1583602A1 EP 1583602 A1 EP1583602 A1 EP 1583602A1 EP 00930914 A EP00930914 A EP 00930914A EP 00930914 A EP00930914 A EP 00930914A EP 1583602 A1 EP1583602 A1 EP 1583602A1
Authority
EP
European Patent Office
Prior art keywords
ultrafiltration
permeate
manure
recited
final
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP00930914A
Other languages
German (de)
English (en)
Inventor
Madeleine Tetrault
Denis Cote
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Purin-Pur Inc
Original Assignee
Purin-Pur Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Purin-Pur Inc filed Critical Purin-Pur Inc
Publication of EP1583602A1 publication Critical patent/EP1583602A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F3/00—Fertilisers from human or animal excrements, e.g. manure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/04—Feed pretreatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/06—Specific process operations in the permeate stream
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/24—Separation of coarse particles, e.g. by using sieves or screens
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
    • Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
    • Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the present invention relates to a method and a system for treating swine manure. More specifically, the present invention is concerned with a method and a system for mechanically dewatering swine manure without the use of chemical additives.
  • An object of the present invention is therefore to provide a new method of mechanically dewatering swine manure with none of the shortcomings of the prior art.
  • Another object of the present invention is to provide a method of dewatering manure that does not necessitate the use of chemical additives for the operation mode.
  • Another object of the present invention is to provide a simple method of dewatering manure that can be automated and, more economically interesting, does not necessitate the use of chemical additives.
  • Another object of the present invention is to provide a method of dewatering manure wherein the liquid output produced therewith can safely be returned to the environment.
  • a further object of the present invention is to provide a method of treating manure that substantially reduces the volume of animal wastes to be disposed of by increasing the percentage of water recovered from the initial manure.
  • a method for treating swine manure comprising mechanically dewatering the manure through a tangential screen having an average pore size between about 200 and 500 microns to obtain a filtrate and a sludge, filtering the filtrate through at least one ultrafiltration membrane to obtain an ultrafiltration permeate and an ultrafiltration concentrate, and filtering the ultrafiltration permeate consecutively through at least one first reverse osmosis membrane and through at least one second reverse osmosis membrane wherein the at least one first reverse osmosis membrane is able to withstand a pressure of between 500 and 1000 psi to obtain a final permeate and a final concentrate whereby the final permeate may safely be returned to the environment.
  • the method above-described further comprises treating the sludge through a press means for separating the sludge into a solid portion containing at least about 25 to 30% of dry solid and a liquid portion.
  • the press means is preferably a screw press but any equivalent may be used.
  • the tangential screen preferably has an average pore size of about 300 microns, and the at least one ultrafiltration membrane used is at least one tubular ultrafiltration membrane.
  • the ultrafiltration permeate is maintained at a temperature not above about 35°C and most preferably at about 20°C.
  • a further step of disinfecting may be added to the above-described methods for treating the final permeate.
  • This step is preferably selected from the group consisting of ozonation and chlorination. It may also be followed by a treatment in an activated coal bed.
  • a system for treating manure comprising a tangential screen having an average pore size between about 200 and 500 microns for separating the manure into a filtrate and a sludge, at least one ultrafiltration membrane substantially removing suspended solids and macromolecules from the filtrate thereby producing an ultrafiltration permeate substantially devoid of suspended solids and macromolecules and an ultrafiltration concentrate, at least one first reverse osmosis membrane able to withstand a pressure of between about 500 and about 1000 psi substantially removing dissolved salts from the first permeate thereby producing a first osmosis permeate and a first osmosis concentrate; and at least one second reverse osmosis membrane substantially removing nitrogen containing molecules from the first osmosis permeate thereby producing a final permeate that may safely be returned to the environment and a second osmosis concentrate.
  • Preferred systems according to the present invention comprise a chiller maintaining the ultrafiltration permeate at 35°C or less.
  • Other preferred systems according to the present invention further comprise a press means for separating the sludge into a solid portion containing between about 25 to about 30% of dry solid and a liquid portion.
  • a press means for separating the sludge into a solid portion containing between about 25 to about 30% of dry solid and a liquid portion There is also provided a system wherein the final permeate constitutes at least 55% of the original manure.
  • raw manure is meant to refer to the manure produced by swine before it is subjected to any treatment. It comprises liquid and solid wastes produced by swine.
  • operation mode is used herein in opposition to the expression “cleaning mode”.
  • operation mode is meant to refer to the manner in which the system described herein is operated during the manure treatment whereas the expression “cleaning mode” is used to refer to the manner in which the system is cleaned.
  • Figure 1 schematically illustrates the steps of a preferred method according to the present invention
  • the overall invention deals essentially with two major phases.
  • the first phase involves the separation of liquids from the swine waste product, to get the driest sludge available, while separating the water for further treatment. This greatly reduces the volume of the sludge once an important portion of the liquid has been removed.
  • the second phase involves the treatment of water and liquid removed from the swine manure.
  • This water is treated by a pressure-driven membrane separation technology so that it is adequately clean environmentally to return to the natural water supply.
  • One of the important features of the invention is that it limits the use of additional chemicals that have been traditionally used to treat sludge to further prevent environmental harm.
  • the invention does not use chemicals, such as chlorine, flocculating or coagulating agents, to obtain an environmentally safe liquid output.
  • chlorine may be used to disinfect the liquid output when it is intended for human consumption.
  • Preferred methods according to the present invention comprise two distinct phases: a liquid/solid separation phase and a liquid treatment phase.
  • the liquid/solid separation phase preferably involves a first screening of the manure with a tangential screen and a screw press. Any press able to produce a solid having a dry solid content of about 25 to 30% can be used without departing from the spirit of this invention. Alternatively, a centrifuge could be used for the liquid/solid separation phase instead of the tangential screen combined with the press when the manure does not contain a high level of swine hair.
  • the size of the pores is selected so that it is able to efficiently screen swine hair and suspended particles and macromolecules. The average size of the pores is about between 250 and 500 ⁇ m depending on the nature of the swine manure to be treated. Preferably, it is about 300 ⁇ m in size.
  • the separated liquid treatment phase involves a number of steps. The filtrate is first conveyed to an ultrafiltration system that removes suspended particles and macromolecules. The resulting permeate contains dissolved organic and inorganic solids.
  • the tubular type of ultrafiltration membrane was determined to be more efficient in screening suspended particles and macromolecules that have a tendency to foul other types of ultrafiltration membranes.
  • the tubular ultrafiltration membrane has the further advantages of being space efficient, compact and of relatively low cost.
  • a high operating pressure is preferably used for treating the ultrafiltration permeate which contains a high concentration of dissolved solids (between 10 000 and 20 000mg/l).
  • the ultrafiltration permeate is therefore preferably conveyed through a first reverse osmosis membrane for a substantial removal of the remaining dissolved ammoniacal nitrogen and other dissolved solids.
  • Figure 1 described below illustrates four first osmosis membranes
  • the methods of the present invention may use one or more first osmosis membrane without departing from the spirit of the present invention depending on the flow of ultrafiltration permeate to treat.
  • the first osmosis permeate obtained according to a preferred method of the present invention could not be immediately rejected in the environment because of the residual amount of nitrogen that it still contains, it could be used as wash-water for the piggery or for general agricultural purposes.
  • the first osmosis permeate is therefore subjected to a second reverse osmosis step to grant the final permeate an improved quality .
  • the operating pressure used during the second osmosis may be between about 200 to 500psi depending on the flow of liquid going through. Under this pressure, about 80 % to 90 % of the flow is able to pass through the second osmosis membrane. The remaining 10 % to 20 % constitutes the second osmosis concentrate, which is returned upstream from the first osmosis.
  • the resulting final permeate constitutes water that is suitable for feeding the swine or may be safely returned to the environment.
  • This final permeate is initially free from adverse bacteria, contamination may occur in the water storage tank which suggests that it may be advisable to disinfect the final permeate taken from the tank before it is fed to swine.
  • the concentrates produced during the treatment can safely be spread as fertilizer.
  • the separated solid retained by the tangential screen can also be conveyed used as a fertilizer. However, due to its high dryness, this solid is very light so that it is preferably mixed with the ultrafiltration or the first osmosis concentrate before it is spread. This solid may also be used for composting.
  • the final permeate produced pursuant to preferred methods according to the present invention may retain a weak odour that is probably due to the small concentration of H 2 S and amino acids that it may still contains.
  • This final permeate is therefore preferably disinfected (chlorination or ozonation followed by an activated coal bed treatment) if it were intended for human consumption to prevent contamination that may have occurred in the water storage tank and to eliminate this odour.
  • Preliminary tests with preferred methods of the present invention have indicated that the use of preferred methods according to the present invention is able to significantly reduce undesirable gaseous emanations produced by swine wastes.
  • any number of screens, ultrafiltration membranes, osmosis membranes depending on the flow of manure to be treated may be used without departing from the present invention.
  • 1 tangential screen, 1 screw press four ultrafiltration membranes, four first osmosis membranes and one second osmosis membrane are preferably used.
  • the volume and quality of the manure produced by pigs in different parts of the world varies depending on the temperature and the nature the food that they are being given.
  • the number of screens, presses and membranes necessary to treat the manure produced a fixed number of pigs may vary according to the place of the world where are grown.
  • FIG. 1 is a schematic view of a preferred method according to the present invention illustrating this method from the liquid/solid separation to the second reverse osmosis step.
  • Example 1 liquid/solid separation of the swine manure
  • raw manure is pumped out of a temporary manure storage tank (1 ) and poured onto a tangential screen (2) having an average pore size of 300 ⁇ m.
  • a portion of the liquid contained in the manure thereby filtrates through the screen so as to produce a concentrated manure portion on the bottom of the screen, a sludge, and a filtrate (5).
  • the sludge is then pressed through a screw press (3) so as to obtain a solid portion (4) and a liquid portion.
  • the liquid portion may be returned to the temporary manure storage tank (1 ).
  • a screw-conveyor (6) then transports the solid portion (4) constituting about two to three percent of the raw manure to storage facilities (not shown).
  • a flocculent solid portion having between about twenty-five to thirty percent of dry solid content and a filtrate (5) having between about two to four percent of dry solid content. It may then be used as fertilizer as it is or mixed with concentrates produced later in the treatment to produce a heavier fertilizer. If a surplus of solid is produced thereby, it can be transferred to an appropriate solid manure treatment center where it may be dried for later exportation. The solid portion can also be used for composting.
  • Example 2 Ultrafiltration
  • the filtrate (5) is then conducted to a filtrate storing tank (34) from which it is led (7) to a tubular ultrafiltration membrane system.
  • a preferred embodiment of the present method uses tubular ultrafiltration membranes for the purpose of substantially removing suspended solids and macromolecules, any type of ultrafiltration membranes may be used without departing from the spirit of the present invention.
  • Four tubular ultrafiltration membranes are separately illustrated and respectively identified as (8a), (8b), (8c) and (8d).
  • the number of membranes used depends on the flow to be treated: for a farm of 5000 pigs, four ultrafiltration membranes are preferably used.
  • This ultrafiltration step produces two principal flows: an ultrafiltration concentrate (10) containing suspended solids and macromolecules strained by the membranes and an ultrafiltration permeate (11 ).
  • the filtrate (7) is preferably divided into two streams (7a) and (7b). Each stream (7a) and (7b) follows a separate but identical path to the other. For instance, stream (7a) goes through the ultrafiltration membrane (8a), the ultrafiltration concentrated portion produced thereby goes through a second ultrafiltration membrane (8b) through (7a').
  • the final ultrafiltration concentrate (10) is brought (10") to a manure storage tank (42) to be used as a fertilizer depending on the level of liquid in the storing tank (6).
  • the ultrafiltration system operates in a semi-batch mode: the ultrafiltration concentrate (10) of the last membrane is returned to the filtrate storing tank (34) so that it is subjected again to the ultrafiltration cycle.
  • the level of liquid in the filtrate storing tank (34) varies during the cycle and sensors (not shown) measure and indicate when the level is high and when it is low.
  • the return of the ultrafiltration concentrate (10) back into the ultrafiltration cycle continues until the level of the filtrate storing tank (34) is high. At that point, the ultrafiltration concentrate (10) is brought to (10") to a manure storage tank (42) to be used as fertilizer.
  • the ultrafiltration concentrate (10) is sent to the manure storage tank (42) until the level of the filtrate storing tank (34) is low: at that point, the cycle starts again and the ultrafiltration concentrate (10) is returned to the filtrate storing tank (34).
  • the ultrafiltration permeate (11) may then be directed to a chiller (15) where it may be cooled to avoid its temperature reaching 35°C to avoid the passage of dissolved salts and nitrogen through the membranes. It is preferably cooled to 20 °C for optimum results.
  • the cooled ultrafiltration permeate (35) is then directed to the first reverse osmosis step.
  • the ultrafiltration permeate may first be conducted (35) to an ultrafiltration permeate storing tank (16).
  • the ultrafiltration permeate storing tank (16) and the osmosis storing tank (22) described below act during the operation mode as temporary tanks for receiving the liquid from the preceding step, respectively the ultrafiltration step and the first reverse osmosis step, ensuring that sufficient liquid will be sent to the next step, respectively the first osmosis and the second osmosis steps.
  • spiral wound polymer membranes of 20,32 cm of diameter are used for the reverse osmosis.
  • reverse osmosis membranes are encompassed by the present invention. Any other type of reverse osmosis membrane able to withstand pressures of 500 to 10OOpsi could be used without departing from the spirit of the invention. The operating pressure was about 5,52 Mpa (800 psi). Tubular reverse osmosis membranes may also be used according to the present invention but they are generally more expensive and are more space consuming.
  • the ultrafiltration permeate is then directed (18) to the first reverse osmosis step.
  • the ultrafiltration permeate goes through a first reverse osmosis membrane (19a) whereby a first osmosis concentrate (20a) and a first osmosis permeate (21a) are produced.
  • the first osmosis concentrate (20a) is then directed to additional concentration steps through additional first osmosis membranes.
  • the number of first osmosis membranes may vary. In Figure 1 , four first osmosis membranes are independently identified as (19a), (19b), (19c) and (19d).
  • the final first osmosis concentrate (20) is directed to the manure storage tank (42) to be used as fertilizer or mixed with other concentrates produced by methods of the present invention.
  • Four streams of first osmosis permeate are illustrated, each one produced by one of the four illustrated first osmosis membranes.
  • the four streams of first osmosis permeate which are each separately identified as (21a), (21 b), (21c) and (21d), are merged and the merged flow (21 ) is led to a reverse osmosis storing tank (22) from which it is directed (24) to the second reverse osmosis step.
  • Figure 1 shows that the first osmosis permeate (24) is then conducted through a second reverse osmosis membrane (26) to produce a second osmosis concentrate (28) and a final permeate (27).
  • the second osmosis concentrate (28) is returned (29) upstream to the ultrafiltration permeate storing tank (16).
  • the final permeate (27) can then be safely returned to the environment or can be led to a water storage tank (33) to be used as wash-water for the piggery, for feeding the swine after a cautionary disinfecting step, or for agricultural purposes.
  • the specific system of the present invention the performance of which was presented in the above examples possesses 1 screen, 1 press, 4 ultrafiltration membranes, 4 first osmosis membranes and 1 second osmosis membrane. It has a capacity of treatment of about 9290 m 3 per year with a variation of about 25%. This performance is calculated on the basis of an operating time of 16 hours per day and of 365 days a year. This system is thereby able to treat efficiently up to 1 ,6 m 3 of manure per hour and 25 m 3 of manure per day. An additional capacity of 25% remains (i.e. six hours each day) and is designed as a safety margin for unforeseeable increases in the manure production and for washing the membranes when necessary.
  • the system may also be adapted for larger farms by increasing the number of membranes operating and/or by using several of the systems presented herein installed in parallel. This specific system was tested on a farm having a manure production of 4736 m 3 per year.
  • Table 1 presents the concentration of various substances of the manure before its treatment and in various outputs of the treatment according to a preferred method of the present invention.
  • Table 2 presents the mineral contents of the final permeate obtained by the preferred method presented in the examples 1 to 3 presented above.
  • the value of fertilizers can be measured in terms of their nitrogen, phosphorus and potassium content: this criterion can be referred to as the N-P-K value.
  • the osmosis and ultrafiltration membranes will be preferably changed every 3 to 5 years.
  • the final permeate (27) is used as wash water for cleaning the ultrafiltration and reverse osmosis membranes.
  • the cleaning mode is conducted countercurrent to the operating mode: the final permeate (27) that is used to clean the second osmosis membrane (26) is reused to clean the first osmosis membranes and this water is then used again to clean the ultrafiltration membrane.
  • the lines (9a), (9b), (9c) and (9d) illustrate how the wash water goes through the ultrafiltration membranes (8a), (8b), (8c) and (8d) in a direction that is countercurrent to the operating mode direction of the liquid to be treated.
  • the pH of the final permeate (27) may be adjusted when it is used as wash water. Any strong acid and strong base may be used to adjust the pH, hydrochloric acid and sodium hydroxide are preferably used because of their low cost and availability.
  • three tanks are used for during the cleaning mode. One of them is used exclusively during the cleaning mode: the filtrate storing tank (34) located upstream from the ultrafiltration receives the filtrate (5) that is still filled with suspended solid and macromolecules. To avoid having to wash this tank before each cleaning mode, a separate tank (12) is preferably used for washing the ultrafiltration membranes (8a), (8b), (8c) and (8d).
  • the storing tanks (16) and (22) have a double function.
  • these storing tanks (16) and (22) act as buffer tanks that ensure that a sufficient amount of liquid from the previous step has accumulated before respectively the first osmosis and the second osmosis step begins. They also act as buffer tanks during the cleaning mode ensuring that a sufficient amount of liquid accumulated before the cleaning of the first reverse osmosis membranes and of the ultrafiltration membranes starts.
  • the washing liquid may be adjusted with various chemical additives to clean the membranes more efficiently.
  • the double function of these storing tanks (16) and (22) reduces the space that would otherwise have been required to locate additional washing tanks. Valves are appropriately located on elements of the system so as to adequately direct the.flow of liquid during the operating mode and the cleaning mode. Hence, the line (17) and other lines illustrated in Figure 1 that have not been referred to in the above examples show the direction of the liquid during the cleaning mode.
  • Both the concentrate and the permeate produced by the membranes during the cleaning mode are sent to the tank (12), (16) or (22) that is situated downstream from them (i.e. during the cleaning mode, the ultrafiltration is located downstream from the osmosis membranes).
  • the washing water coming out of the ultrafiltration membranes (8a), (8b), (8c) and (8d) is sent to the temporary manure storage (1 ).

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Nanotechnology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un procédé de traitement de fumier de porc consistant à déshydrater manuellement le fumier au moyen d'un tamis tangentiel ayant un diamètre moyen de pores de 200 à 500 microns afin d'obtenir un filtrat et une boue, à filtrer le filtrat au travers d'au moins une membrane d'ultrafiltration afin d'obtenir un perméat d'ultrafiltration et un concentré d'ultrafiltration, et à filtrer le perméat d'ultrafiltration au travers d'au moins une première membrane d'osmose inverse et d'au moins une deuxième membrane d'osmose inverse, la ou les premières membranes d'osmose inverse pouvant supporter une pression de 500 à 1000 psi, afin d'obtenir un perméat final et un concentré final, le perméat final pouvant être retourné à l'environnement de manière sûre. La présente invention concerne également un système de traitement de fumier comportant les éléments destinés à la mise en oeuvre du procédé selon l'invention. Le fonctionnement desdits système et procédé de traitement de fumier ne nécessite pas d'additifs chimiques.
EP00930914A 2000-05-19 2000-05-19 Procede et systeme de traitement de fumier de porc Withdrawn EP1583602A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CA2000/000598 WO2001087467A1 (fr) 2000-05-19 2000-05-19 Procede et systeme de traitement de fumier de porc

Publications (1)

Publication Number Publication Date
EP1583602A1 true EP1583602A1 (fr) 2005-10-12

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP00930914A Withdrawn EP1583602A1 (fr) 2000-05-19 2000-05-19 Procede et systeme de traitement de fumier de porc

Country Status (3)

Country Link
EP (1) EP1583602A1 (fr)
AU (1) AU4904200A (fr)
WO (1) WO2001087467A1 (fr)

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ES2301346B1 (es) * 2006-03-24 2009-05-01 Polinox Galicia S.A. Maquina para la obtencion y depuracion de agua contenida en residuos.
WO2009021552A1 (fr) * 2007-08-13 2009-02-19 Eco Flanders Procédé/installation améliorés de séparation/épuration pour dispersions aqueuses liquides de matières organiques, et utilisation de tels procédés/installations dans le cadre d'un traitement intégré du fumier et/ou des digestats organiques
DK177918B1 (da) * 2008-05-07 2015-01-05 Purfil Aps Fremgangsmåde og apparat til behandling af gylle og ajle fra husdyr, samt biologisk belastet spildevand.
BE1018011A3 (nl) * 2009-02-12 2010-03-02 Eneco En Internat B V Verbeterde scheiding/zuivering methode/installatie voor waterige vloeibare suspensies van organisch materiaal en het gebruik van een dergelijke methode/intallatie in een geintegreerde behandeling van mest en/of organische digestaten.
IT1400942B1 (it) * 2010-06-23 2013-07-02 Kron Morelli Impianto e procedimento per l'estrazione di azoto ammoniacale da reflui liquidi, particolarmente per la riduzione della quantita' di refluo destinata allo spandimento
ITCR20130027A1 (it) * 2013-10-22 2015-04-23 Rota Guido Srl Processo in discontinuo di riduzione dei volumi di spandimento e del contenuto di azoto in liquami zootecnici
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CN106746012A (zh) * 2016-12-30 2017-05-31 北京桑德环境工程有限公司 一种市政给水深度处理系统及方法
CN110342772A (zh) * 2019-06-27 2019-10-18 江苏连昌环保设备有限公司 奶牛养殖场污物处理装置及其处理方法

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