KR100348438B1 - Waste Material Treatment Plant and Process - Google Patents

Abstract

The present invention passes through a bioreactor system comprising a plurality of bioreactors connected in series with waste containing animal or human manure containing insoluble components such as lignocellulosic and removing the insoluble components from the waste. Maintaining in suspension; And (ii) filtering the insoluble components from the waste to appropriately separate. The present invention also provides a bioreactor system comprising (i) a number of bioreactors connected in series for treating waste; (Ii) It also provides a waste plant comprising means such as a filter for separating insoluble components from the waste after passing through the bioreactor system.

Description

Waste Material Treatment Plant and Process

Disposal of waste materials, including large-scale commercially operated pig farms, beef feed sites, livestock feed sites, cattle farms, including dairy dairy areas, and faeces from poultry farms The process has been expensive. This often occurs due to problems with the effective treatment of insoluble or undigested solid or sludge components formed from manure of animals mixed with feed of undigested livestock. Animal manure includes proteins, proteolytic products, fats, complex carbohydrates, and lignocellulose. Lignocellulosic is an amorphous matrix of hemicellulose and lignin. Hemicellulose is usually polysaccharides produced from sugar and uronic acid. Lignin is a highly cross-linked aromatic polymer that does not have regularly repeated units because it is produced by the aggregation reaction of free radicals. Lignocellulosic in animal manure is derived from barley, lucerne, sorghum and other livestock feed.

Australian patent application 91080/91 (International Patent Application PCT / AU91 / 00587 Publication No. WO 92/11210) discloses a reinforcing layer of biological waste material consisting of two soft reticular polyurethane foam layers and a synthetic material positioned between them. A waste material treatment process is described that includes passing through one or more hanging curtains formed from layers. The curtain forms a support for fibrous micro-organisms that forms a mat of dense cellular material. Micro organisms remove dissolved phosphorus in the form of ammonia and dissolved carbon in the form of nitrogen and organic acids from biological waste materials.

The process in WO 92/11210 is very efficient in treating not only glycerol waste, but also biological waste from distillery and beer breweries, which waste and animal feed site wastes, as described above. This requires a necessary early anaerobic fermentation step. Non-fermented biological wastes, as described in WO 92/11210, are introduced into an anaerobic fermentation step to clearly decompose complex macromolecules such as carbohydrates, proteins, lipids into organic acids having up to 8 carbon atoms. This fermentation step usually takes place in the presence of acidogenic fermentable bacteria to produce organic acids such as volatile fatty acids that can be easily metabolized to carbon dioxide by the rinsing curtain technique described above.

The supernatant soluble and extinguishing material was collected and generally separated from the insoluble or undigested sludge components described above, including lignocellulosic, after the completed fermentation step, typically at least 5 days later.

Conventional methods of treating non-digestible materials include passing the non-digestible materials through anaerobic ponds, septic tanks or pits. Optionally non-extinguishing material was dehydrated by filtration or drying on open or covered sand beds. The dry sludge described above was substantially incinerated or used as fertilizer. In some cases, non-extinguishing materials were used for landfill.

However, the presence of non-digestible materials in anaerobic fermentation tanks or digesters means that fermentation should be stopped at regular time intervals to remove time-consuming and expensive and non-digestible materials. You can guess.

The above non-extinguishing materials also cannot be spread on anaerobic ponds or used as landfills in Islamic countries such as Malaysia or Indonesia. In countries where this is possible, transportation costs are relatively high.

The presence of non-digestible substances in the anaerobic digester is also undesirable because it accumulates in the digester for a certain time and produces a phenolic compound, which inhibits the efficient progression of the fermentation reaction. The above compounds are also toxic to the fibrous micro-organisms used in the henling curtain technology of International Patent Publication WO / 9111210.

It is also contemplated that non-digestible material contains many pathogenic micro-organisms after an anaerobic fermentation step that does not completely remove prior to causing illness or infection by pumping or spreading non-digestible material into anaerobic ponds as a slurry. Can be.

To eliminate this possibility, the pH of non-digestible materials is reduced to less than pH 4.5 (pKa of volatile fatty acids) as suggested by Henry et al., Journal Appl. Bact. 55, 89-95 (1983). It is necessary to let. In this connection it can be seen that free volatile fatty acids can eliminate bacterial pathogens.

The present invention relates to waste material processing plants and processes.

Preferred embodiments of the invention are presented as shown in the accompanying drawings.

1 is a flowchart constituting a waste material processing plant according to the present invention;

2 is a flow chart of a waste treatment plant constructed in an alternative form according to the present invention.

[Detailed description]

In FIG. 1 a holding tank 10 on the ground is shown for an inlet comprising manure mixed with undigested or waste feed from a pig farm (not shown). The inflow is pumped by a feed pump 11 and passes through an emulator 12 which breaks the particles in the inflow into small particles or finely cut material and the inflow is mounted to a bearing 16. Pass through bioreactor 13 with stirrer 14 with shaft 15. Also provided is a conduit 17 between the holding tank 10 and the emulsifier 12, a conduit 18 between the feed pump 11 and the emulsifier 12 and a conduit 19 to allow interconnection between the inlet conduit 20 and the bioreactor 13. Conduit 20 provides a shut off valve V ₁ and a flow control diaphragm valve V ₂ . Conduit 21 acts as a return line in which the inlet flows back from bioreactor 13 through conduit 20 back to holding tank 10, which is governed by the operation of valves V ₁ and V ₂ .

It also provides additional bioreactors 13A, 23B, 13C, 13D and 13E that are similar in structure to Bioreactor 13. Overflow conduits 22 are provided for transferring fluid between adjacent bioreactors. Each bioreactor is provided with a drain line 23 having a short off valve V ₁ .

Steam boiler 24 is provided where raw water is introduced through conduit 25 to single valve V ₁ . Steam passes through a conduit with a pressure control valve assembly 27.

A plurality of steam conduits 28 are also provided that are interconnected to respective supply conduits 26 that pass steam through each of the bioreactors 13-13E. Each steam conduit 28 is also provided to the vacuum grinder valve V ₃ as shown to stop siphonage of the fluid. Temperature control valve in the form of a sliding gate valve connected to conduit 30 having a thermometer regulator 31 which is a thermometer or a probe that extends to each bioreactor to control the temperature at each bioreactor 13 to 13E. Short off valve V ₁ is provided in each conduit 28 as well as other valves V ₁ connected to 29.

Outlet conduit 32 is provided to each of the bioreactors 13-13E interconnected to conduits 33 to allow effluent gas to flow into tanks 48, 50, and 56 through transport conduits 32A and inlet conduits 33A, 33B, and 33C. Do it. The effluent gas can then pass through return line 34A to a pair of gas stubs 34 connected in parallel as shown from gas line 49A. The bottom gas scrubber 34 has a conduit 35 connected and the top gas scrubber 34 has a conduit 36 connected. Conduits 35 and 36 are shorted to valve V ₄ and connected to conduit 37 interconnected to fan 38 and stack 39. A steam trap 40 is also provided. Valve V ₄ functions one scrubber 34 to hold.

The effluent passes through the final bioreactor 13E and then through feed pump 41 through conduit 42 and substantially through conduit 43 through sludge filter 44. Pressure indicator 51 is shown to be connected to conduit 43 as well as conduit 47. The solid fraction 45 of the sludge filter 44 is held in a vessel 46 where the solid fraction 45, predominantly lignocellulosic, is delivered by truck 46A for incineration or other forms of treatment. The contaminant, which was then enriched with volatile fatty acids or VFAs, was maintained for two days before passing through conduit 52 through transfer pump 53 and through VFA holding tank 50 through conduit 52 connected to conduit 55. Pass through 47 to VFA feed tank 48.

Conduit 28A is connected from the sulfuric acid feed tank 57 which is connected to inlet conduit 58 having a pressure relief valve V ₅ and drain conduit 59 interconnecting steam from conduit 26 to conduit 62 passing through sulfuric acid pump 60. It functions to deliver VFA liquid acidification tank 56 injecting sulfuric acid. A sump 61 is also provided. The sulfuric acid passes through conduit 62 which is connected to conduits 58 and 59 in an acidification tank 56 provided with agitator 14 as shown. Each stirrer 14 and associated tank 56 as well as shaft 15 of the bioreactors 13-13E are provided for variable speed regulation (VS), expressed in phantoms. The material is transferred from tank 56 via conduit 49 through conduit 52 to conduit 55 and to tank 56 via conduit 57 which is dependent upon the operation of short off valve V ₁ .

Conduits 64, 63 and 65 are also provided respectively connected to tanks 48, 56 and 50 for delivering effluent gas to gas line 49A and substantially flowing to return line 34A. Conduit 67 degrees It is shown that it has a thermostat 31 to control the temperature of the tank 56. Conduit 67 is connected to conduit 28A via a temperature control valve 29 as shown.

Tank 50 is also provided to the temperature indicator 68 and tank 56 is also provided to the pH indicator as shown.

The solution emanating from the VFA holding tank 50 is passed through conduit 71 to a hanging curtain assembly 70 and to a curtain feed pump 72 provided with a variable speed control VS. Conduit 71 is separated into conduits 73 and 74, 75 and 76 as well as 77 and 78 providing liquid waste, as shown on one side of the curtain module or curtain sub-assembly 79A. Three additional sub-assemblies 79B can be used if needed to increase the waste treatment capacity of the rinsing curtain assembly 70. The flow connection from sub-assembly 79B to pump 72 has been omitted for clarity. Each of sub-assemblies 79A and 79B is contained within a housing 80 that includes an inclined drain floor 81. Also used was a temperature recorder 82 connected to the housing 80.

The gas exiting the housing 80 passes through the conduit 83 through the damper valve V ₆ , the cooling fan 84 and the stack 85. Another brake V ₆ is also presented which is connected to the outside of the housing 80 and operates each brake valve V ₆ to regulate the air flow through the housing 80. The air pressure inside the housing is preferably kept below atmospheric pressure.

The waste effluent is passed from the inclined floor 81 of the housing 80 to the treated waste holding tank 86 including the discharge pump 87 connected thereto via a conduit 86A. Also provided is a level element 91 that regulates the pump 87 to maintain the level of fluid in the housing 80. pH indicator 89 is also provided. The fluid is pumped through the discharge conduit 88, which includes a return line 89A by a pump 87. Waste is recycled from conduit 88 to housing 80 as shown through conduit 90. The waste is then passed to treatment pond 92 connected to another pond 93 via conduit 94 using pump 95. The waste is then transported to feed tank 96 via conduit 97. Conduit 97A then transfers the fluid to the treatment channel or plume of the pig farm. The fluid is then conveyed to holding tank 10 via bypass plate 99 or optionally including a discharge pump 102 that transports fluid through conduit 100 through conduit 103 to treatment pond 92. Transported to a ground holding tank 101.

In an optional arrangement, as indicated by the phantom, the material spilled from the conduit 88 passes through the conduit 104 and is transported to the filter 105 so that the solid portion 107 is placed in a container before being removed by incineration or other forms of treatment truck 108A. Deposited during 106. The liquid portion passes through conduit 105A and moves from filter 105 to liquid tank 108 via via conduit 109 and recycled to plum 98 by pump 110.

2 shows an improved waste treatment plant compared to the waste treatment plant shown in FIG. 1. The same reference number is used for convenience. One difference between the FIG. 1 plant and the FIG. 2 plant is the application of bioreactors 13-13F on the slope as shown using the overflow conduit 22 to facilitate the transport of fluid from adjacent bioreactors. The valves are not shown for convenience. One conduit 18 is connected to the storage tank 10 and the bioreactor 13 and the steam exiting the boiler 24 flows through the conduit 26 and then through the inlet conduit 28 to each bioreactor 13-13F. The outlet conduit 32 for gas is also connected to the main transport conduit 33 as described in FIG. 1 waste treatment plant.

Gas is passed through conduits 33 to acidification tanks 56A and 56B, and as shown, through inlet conduits 33A and 33B to each tank. Gas is also provided to gas scrubber 34 on return line 34A.

As a variant of the method shown in FIG. 1, after discharging from the final bioreactor 13F, the waste eluate or waste material can be transported directly to acidification tank 56A through conduit 44A as indicated by the phantom. In this variant, the waste material still contains insoluble components transferred to it, and after passing through conduit 45A, also referred to as phantom, the waste material is transported from acidification tank 56B to filter 44. After filtration, the liquid portion is then passed through conduit 46A, also represented by phantom, to the curtain assembly 70.

Another difference is the application of two VFA liquid acidification tanks 56A and 56B to pass the liquid portion from the sludge filter 44 through conduit 47 and then through tank 56A. Sulfuric acid is pumped from tank or drum 57 to tank 56A via conduit 62 by pump 60. Material can then be transferred from tank 56A to tank 56B through conduit 62A. The acid treatment fluid may then flow through the conduit 71 to the curtain assembly 70.

After flowing through the curtain assembly 70 the waste liquid flows through the conduit 86A and into the filter feed tank 86, after which the fluid passes through the conduit 104A and then through the conduit 88 by the pump 87 to the treatment pond 92 or the recycling conduit 90 It is pumped through to the curtain assembly 70. The liquid flowing out of pond 92 flows through plumb 97 back into plume 98 using pump 95. The fluid can also be passed through conduit 104A to the filter 105 from the curtain assembly 70 such that the liquid portion can flow through the conduit 105A to the treatment tank 108, after which the fluid flows through the conduit 109 through the conduit 109 and into the conduit 97. Can be.

Waste that flows through a series of bioreactors is continuously broken down by different plant contaminants in each tank. The short means remaining time (~ 24 hours) in each tank allows the particular plant to grow in each tank to gradually break down the transported material The final result is volatile fatty acid products (VFAs), for example C ₂ − Product of C ₈ (acetic acid, propionic acid, butyric acid, valeric acid, caproic acid, heptanoic acid, octanoic acid and similar isomers). Non-volatiles such as lactic acid and / or succinic acid were not used, trace amounts of ˜3 mM- ¹ phenylacetic acid were observed, limiting the final product of the fermentation to obtain VFAs. The purpose is to show the effect on the destruction of bacterial pathogens present in the waste.

Continuous fermentation also allows conditions of pH, fermentation and remaining time to maximize production of VFAs in each bioreactor maintained.

It is therefore an object of the present invention to provide a process and plant for waste treatment to alleviate some of the above problems with regard to the efficient treatment of insoluble or non-digestible sludge components including lignocellulosic.

The process of the present invention comprises the following steps:

(i) passing the waste material comprising insoluble components through a bioreactor system comprising a plurality of bioreactors arranged in a line to maintain the insoluble components in a suspension in the waste material;

(ii) separating the insoluble component from the waste material;

Process.

And (i) a bioreactor system comprising a plurality of bioreactors arranged in a line for treatment of waste materials;

(ii) means for separating insoluble components from the waste material after passing through the bioreactor system;

It also includes a waste treatment plant.

The waste material introduced into the process of the present invention is preferably manure from the livestock feed site described above, which may suitably comprise human or animal manure and may comprise livestock feed ingredients including lignocellulose.

Each bioreactor is connected by a transport conduit so that waste material or influent is quickly and efficiently transported from one bioreactor to the adjacent bioreactor without the need for pumping material. Interconnect to the reactor.

It is appropriate to provide agitation means in which the components of each bioreactor are kept in the form of a slurry or suspension so that the solid particles remain in suspension to obtain the material of the present invention.

The components of each bioreactor are also appropriately applied to appropriate heating means and in one form may be provided as steam passed into and out of each bioreactor. However, other forms of heating means can be utilized for electrically heating. The temperature of each bioreactor is preferably maintained at a temperature of 25 to 50 ° C. and more preferably 30 to 40 ° C., which is a preferable temperature by means for automatically and automatically adjusting the temperature.

In a preferred embodiment the temperature decreases slowly from the initial 40 ° C. to the final 30 ° C. as the waste passes through each bioreactor.

The pH of the waste material injected into the bioreactor is preferably maintained between 5.0 and 7.0 and more preferably between 5.8 and 6.4. The reaction time of each bioreactor is 12 to 48 hours, more preferably 24 hours.

If the waste effluent is removed from the bioreactor system and then the insoluble material, preferably incinerated through a filter or sieve, is filtered or spread on the ground, acidification tanks will be described later. Pass it through. It can be expected that the insoluble material is removed in an appropriate manner. Filtration is a preferred process and flocculation can also be utilized.

The soluble liquid of the supernatant or filtrate is passed through one or more acidification tanks and maintained in the tank for 24 to 48 hours to maintain a pH of 4.5 or less and more suitably acetic acid, propionic acid, butyric acid. (butyric acid), valeric acid (valeric acid), caproic acid (caproic acid), enanthic acid (enanthic acid), octanoic acid, as well as 4.0 to 4.5 below the pKa value of volatile fatty acids such as isomers Decrease. These volatile fatty acids (VFAs) are produced by anaerobic bioreactor systems and when the pH is lowered, the VFA salts in the acidification tank are converted to free acids. This is not for all bacterial pathogens, but is the best way to get rid of them.

As a transformation of the process described above, in some cases the waste effluent is removed from the bioreactor system and then passed through the acidification tank to remove the insoluble components. In this embodiment, after removing the insoluble material, the waste effluent passes through a curtain assembly, which will be described later. This process is preferred when it is not possible to incinerate the insoluble material after the waste material has passed through the bioreactor system and filtered.

Means may be provided for maintaining an atmosphere of carbon dioxide or other gas in the acidification tank to inhibit the growth of yeast in the acidification tank. Such means may include, for example, conduits for expanding carbon dioxide or other gas into each acidification tank. The conduit can be connected to a suitable source of carbon dioxide or other gas.

In such an embodiment, it is desirable to provide a means such as suitable conduits for transporting the effluent gas (which may include carbon dioxide) produced in the bioreactor system to the acidification tank to maintain the waste material in an acidified gas atmosphere. Do. These features described above are useful for inhibiting the growth of yeast or fungi such as Candida ingens in acidification tanks. The gas can be removed with a gas scrubber for final release from the acidification tank by substantially suitable conduits.

The waste material is preferably subjected to further treatment to remove carbon in ammonia form nitrogen, dissolved phosphorus and volatile fatty acids. More preferably, a suitable means for removing nitrogen, dissolved phosphorus, and carbon in the form of ammonia is a rinsing curtain assembly. In this particular embodiment, the waste from the acidification tank can be passed through a rinsing curtain assembly, wherein the rinsing curtain assembly is of the type described in, for example, patent 91080/91. The carbon may be released as carbon dioxide to remove the and carbon from the waste material. The carbon releases carbon dioxide so that the residue is retained by micro-organisms in the rinsing curtain assembly.

Claims (29)

(Iii) passing the waste material comprising insoluble components through a bioreactor system comprising a plurality of bioreactors connected in series to maintain the insoluble components in suspension in the waste materials; (Ii) transferring the treated waste material from the bioreactor system to one or more acidification tanks to reduce the ph to 4.5 or less to produce free volatile fatty acids for removing bacterial pathogens in the treated waste material; And (iii) a process for separating the insoluble component from the waste material before or after step (ii) Waste treatment method comprising a. The method of claim 1, further comprising a waste material treatment process for removing carbon as nitrogen, dissolved phosphorus, and volatile fatty acids in ammonia form. The method of claim 1, wherein the waste material is agitated in each bioreactor such that the waste material remains in the form of a slurry or suspension such that the insoluble component remains suspended. The waste treatment method of claim 1, wherein the waste material is heated to a temperature of 25 to 50 ° C. in each bioreactor. The waste disposal method of Claim 4 which maintains the said temperature at 30-40 degreeC. The method of claim 5 wherein the initial temperature of the waste material in the bioreactor system is 40 ° C. before the temperature slowly decreases to 30 ° C. 7. The method of claim 1 wherein the bioreactor system maintains a pH between 5.0 and 7.0. 8. The method of claim 7, wherein said ph is maintained between 5.8 and 6.4. The waste treatment method of claim 1, wherein the waste material is left in each bioreactor for 12 to 48 hours. The waste disposal method of claim 9, wherein the waste material is left in each bioreactor for 24 hours. The method of claim 1, wherein after removing the waste material from the bioreactor, the filter or sieve is passed through to filter out insoluble components. 12. The method of claim 11, wherein the remaining liquid portion is passed into one or more acidification tanks for 24 to 48 hours after removing the insoluble components. 3. The waste treatment of claim 2 wherein said waste material is passed through a rinsing curtain assembly for removing carbon as nitrogen, dissolved phosphorus, volatile fatty acids in ammonia form after passing through said at least one acidification tank. Way. The method of claim 1 wherein said pH is reduced to a value between 4.0 and 4.5. The waste treatment method according to claim 1, wherein each acidification tank maintains a carbon dioxide or effluent gas atmosphere to suppress the growth of bacterial pathogens. (Iii) a bioreactor system comprising a plurality of bioreactors in series for treating waste material; (Ii) one or more acidification tanks for reducing the pH below 4.5 to form free volatile fatty acids for bacterial pathogen removal in the treated waste material; and (iii) means for separating insoluble components from the waste material after passing through the bioreactor system Waste treatment plant comprising a. 17. The waste disposal plant of claim 16, wherein each bioreactor is connected to adjacent bioreactors by transport conduits. 17. The waste disposal plant of claim 16, wherein the starting bioreactor is located at a higher position than the final viroactor and each of the bioreactors is inclined. 17. The waste disposal plant of claim 16, comprising heating means in each bioreactor to maintain an operating temperature of 30-40 ° C. 20. The waste disposal plant of claim 19, wherein the heating means comprises means for injecting steam into each bioreactor. 21. The waste disposal plant of claim 20, further comprising a steam boiler connected to a steam conduit connected to an injection conduit connected to each bioreactor. 20. The waste disposal plant of claim 19, comprising constant temperature control means to maintain the operating temperature in each bioreactor. 17. The waste disposal plant of claim 16, wherein each bioreactor includes agitation means to maintain the waste treatment material in suspension. 17. The waste disposal plant of claim 16, wherein the separation means comprises a filter or sieve for separating insoluble components from the liquid portion of the waste material. 17. The waste disposal plant of claim 16, comprising means for maintaining an atmosphere of carbon dioxide or other gas in the acidification tank (s) to inhibit growth of yeast. 26. The waste disposal plant of claim 25, wherein the means for maintaining a carbon dioxide atmosphere comprises transport means for transporting the effluent gas generated in the bioreactor system to the acidification tank (s). 27. The waste disposal plant of claim 26, wherein the gases exiting from the acidification tank (s) are transported to an offgas scrubber. 17. The waste treatment plant of claim 16, further comprising treatment means associated with one or more acidification tanks to remove carbon as ammonia in form of ammonia, dissolved phosphorus and volatile fatty acids. 29. The waste disposal plant of claim 28, wherein the processing means comprises a rinsing curtain assembly.