HU196343B - Process and plant for the biological decomposition in anaerobic way of organic material to be found in organic material-containing liquids, particularly in sewage or in liquid manure - Google Patents

Abstract

The anaerobic reactor (1) has a lower density than water, covered with a biofilm containing microorganisms particulate material (18) floats and the liquid to be treated from below upwards on this granular material across. Granules containing biofilm (18) a retaining device formed by a mesh or grid (9) held in the contact bed biological reactor (1). These retention devices are the treated fluid the funnel (s) (8) for removal.

Description

FIELD OF THE INVENTION The present invention relates to a process and apparatus for anaerobically biodegrading organic matter in an organic liquid, especially waste water or slurry.

The treatment of municipal and agricultural wastewater and industrial wastewater containing organic matter is essentially the biological degradation of organic pollutants.

During biological wastewater treatment, organic pollutants are decomposed by aerobic or anaerobic routes.

The essence of aerobic biological wastewater treatment is that the biocatalysts produced by the microorganisms with the dissolved oxygen introduced into the wastewater oxidize or partially integrate the biodegradable organic carbon into microorganisms with high energy release. This process is relatively fast - but in less than a day, the disadvantage is that oxygenation requires a lot of energy and results in high cell growth and high sludge production.

During anaerobic biological wastewater treatment, the pollutant organic matter is eventually reduced to methane gas, also by biocatalysts produced by microorganisms. Methane gas can be used as an energy carrier, and relatively little energy is spent on cell growth. Thus, sludge production is low, but because of the slow growth of methane-producing bacteria, the wastewater will have to remain in the floating sludge anaerobic biological reactor for a long time, usually several days. However, only effluents with thousands of mg / l of BOD can be effectively treated anaerobically because less contamination does not provide the required cell mass (cell concentration) and methane production is not sufficient to provide optimal temperatures for microorganisms. Therefore, despite its undoubted advantages, anaerobic wastewater treatment technology is used only for wastewater with high organic matter content and in very simple cases, especially for the partial treatment of wastewater from family houses and holiday homes. in pools or shafts. They are usually composed of three series-connected chambers with anaerobic degradation during a residence time of 5 to 10 days (extended dissolution pool), but with a purification efficiency of only 30-40% BOD. A simple (single-chamber) manhole with only three days of wastewater - so essentially only mechanical cleaning - provides only 25-30% cleaning efficiency. However, purification of high organic matter wastewater in anaerobic reactors achieves a purification efficiency of 75-80%. Since there is no significant difference in the residence time between the two anaerobic wastewater treatment processes (reactor and reactor) - and even the residence time for high organic matter wastewater treatment, especially at higher temperatures - the significant difference in purification efficiency is only due to the high concentration of sludge. -differentiation. Due to the extremely low water flow and the sedimentation nature of these artefacts, the sludge concentration in the water space is very low, while the anaerobic digestion of residual sludge due to anaerobic purification of high organic matter effluents using various hydraulic methods: for example, mixing the contents of the anaerobic reactor completely; either the recirculated sludge is recirculated or the recycled wastewater is rotated to create a flow rate in the reactor that keeps the sludge floating. The effect of these methods is limited, however, because they cannot produce activated sludge concentrations greater than 5-10 kg / m ³ , but they still greatly improve the efficiency of anaerobic wastewater treatment.

Anaerobic wastewater treatment plants with a bed of solid particulate material, such as a gravel filter, are also known. In these fixed bed (fixed bed) anaerobic filters, e.g. the biomass adhering to the gravel bed decomposes organic contaminants. Such anaerobic filters also provide concentrations of 15 to 20 kg / m ^{3 of} cleven sludge and can achieve an 80% effective decomposition of organic matter in 5 to 6 days. However, they have the serious disadvantage that they are only capable of treating pre-treated wastewater and are still clogged up over time, so they need to be periodically regenerated, which requires shutdown of the reactor, plus energy and labor-intensive regeneration! to execute. Obviously, this can be done with a simple cleaning device such as a cleaning device. the expanded anaerobic leach basin, practically no option at all.

It is an object of the present invention to provide a process and apparatus for the naeobic decomposition of organic matter in organic liquids, particularly wastewater and slurry, which results in a higher concentration of activated sludge in the known floating sludge anaerobic reactors, provides smaller organic matter concentrations but does not require system management, e.g. which is essential for anaerobic wastewater filters.

The present invention is based on the discovery that, when a floating contact bed of a biofilm-coated floating bed of particulate matter is formed in an anaerobic biological reactor, the hydraulic methods of sludge concentration increase and the same an high sludge concentrations can be achieved as in anaerobic wastewater filters, but the hydraulic component of such a system is no different from floating sludge cloud anaerobic biological reactors.

Based on this discovery, the object of the present invention has been solved by a process for decomposing organic material into methane in micro-organisms in an oxygen-free environment, characterized in that the decomposition is carried out by the organic layer containing passing through a bottom-up stream of particulate matter of less density than water floating in the liquid. It is preferred that the organic fluid contains 0.8 to 1.0 g / cm ³ , preferably 0.9 to 0.95 g / cm ³

196 34.1 density; It is passed through a particulate material having a particle diameter of 4 to 20 mm, preferably 5 to 10 mm, preferably 200 to 500 kg / m ³ , preferably 300 to 350 kg / m ³ , such as pre-expanded polystyrene beads, polyethylene or polypropylene granules, rubber flour or the like.

The apparatus for carrying out the process according to the invention has a closed container with an opening-closure orifice, at least one reactor compartment, pipes for feeding the liquid to be treated and discharging the treated liquid, and a gas outlet, and the apparatus has the a lower density bio-layer of microorganisms! is provided with a funnel located below the fluid level in the upper portion of the reactor compartment, containing a device for retaining the particulate material, and a tube for supplying the liquid to be treated to the lower portion of the reactor compartment. A biological reactor is a closed container, manhole, basin or similar enclosure with a practically attractive layout, bounded by a vertical mantle or sidewalls, which has no internal structure other than the funnel.

In a preferred embodiment of the apparatus, the reactor space is formed in a closed container having a cylindrical side wall and a conical bottom and lid; at the end of the fluid supply tube there is a downwardly tapered manifold which is located in the upper part of the container for the discharge of the treated liquid. In this case, it is desirable to have a sludge discharge pipe from the vicinity of the deepest part of the reactor space and a gas discharge pipe from the vicinity of the highest point of the tank.

In another embodiment, the apparatus has a settling space and a plurality of reactor spaces; a tube for feeding the fluid to be treated to the upper portion of the settling chamber; a settling tube is connected to a first reactor space by an eccentric tube, the tubular member of which in the first reactor space extends to the bottom of this reactor space; the first reactor space being connected to the second reactor space by a conduit having a funnel having a particulate material retention means in the first reactor space, and a second member of the second reactor space extending to the bottom of this reactor space and, lastly, the a treated fluid removal tube terminating in a funnel with a particulate material retention device; preferably, the reactor has a cylindrical vessel in which the settling space is semicircular and the reactors are quarter-circular.

In another embodiment of the apparatus, the reactor space or compartments have a density of 0.8 to 1.0 g / cm ³ , preferably 0.9 to 1.95 g / cm ³ , 4 to 20 mm, preferably 5 to 10 mm. Floating particulate material having a particle diameter of 200 mm, preferably 200-500 kg / m ³ , preferably 300-350 kg / m ³ , for example, pre-expanded polystyrene beads, polyethylene or polypropylene granules, or rubber granules.

Finally, it is desirable that the funnel retaining structure of the funnel is provided with a mesh braid or grid having a mesh size smaller than the particle diameter of the particulate material.

The invention will now be described in more detail with reference to the accompanying drawings, which show a preferred embodiment of the apparatus. In the drawings, Figure 1 is a schematic vertical sectional view of an embodiment of the apparatus;

Figure 2 shows another embodiment; 3 is an enlarged schematic drawing of a vertical sectional view taken along the line B-B in Figure 3;

Figure 3 is a horizontal sectional view taken along line A-A in Figure 2.

The apparatus of FIG. 1 is provided with a cylindrical anaerobic biological reactor, denoted as 1, in its entirety, having a closed container x having a central vertical geometric axis x, closed at its bottom by a conical bottom 2 and also by a conical lid 3. The latter has openable and lockable 4 cleaning installation openings (manhole). Such a cleaning-installation opening 4 also extends into the lower part of the cylindrical part of the reactor 1, just above the bottom 2.

A crude fluid feed tube 5 is introduced into the lower portion of the reactor 1 and has a downwardly facing head 5a in a vertical geometric central axis x which directs the fluid stream downwardly.

From the deepest region of the conical bottom 2, a sludge discharge pipe 6 is led outside the reactor 1.

From the upper part of the reactor 1, a cleaned fluid drainage tube 7 is discharged, to which is attached a funnel 8 facing upwardly inside the reactor and having a particle retention device 9 in its upper opening. Floating material having a density less than water itself is designated by reference numeral 18. The vertical geometric center axis of the funnel 8 coincides with the vertical vertical axis x of the reactor 1. The upper edge of the funnel 8 is located below the liquid level v in the reactor 1. The particulate retention device 9 is e.g. it is formed by mesh battens, grids or the like having a particle size of less than 18.

From the vicinity of the highest point of the conical lid 3, a vent pipe 10 is led outside the reactor 1.

Figures 2 and 3 show an embodiment of the apparatus which is analogous to a known three-chamber anaerobic expanded dissolution basin, but of course is constructed and operated according to the invention. The anaerobic reactor is referred to herein as a whole by reference numeral 11, the cylindrical portion x of which has a vertical geometric center axis closed at the bottom by a flat bottom 24 and a conical lid 23 having a pivotable, multifunctional central opening 20 around its highest point.

The interior of the All Reactor is divided by vertical radial bulkheads 21, 22 into a semicircular sedimentation space 13 and two quaternary-shaped reactor space 15.16. A raw liquid feed tube 12 extends tangentially to the upper portion of the settling chamber 13. The settling chamber 13 is connected to the reactor space 15 by a decanter tube marked 14 throughout. The decanalization tube 14 has a horizontal tube member 14b extending at a liquid level v across the upper end region of the bulkhead 21, extending from a shorter tube portion 14a extending vertically in the sedimentation space 13 to a lower portion of the reactor space 15 11 reactor

196 342 (located near the bottom of cl 5). The upper end of the tubular members 14a, 14c extends above the liquid level v.

Between reactor compartments 15 and 16, the fluid transport conduit 17 extends through the rectifier space 16. it has a vertically extending tubular member 17c having a lower end near the bottom 24 and an upper end above the liquid level v. From the tubular member 17c, a horizontal tubular member 17b is branched through the septum 22 to the reactor space 15 and is connected to the end of the tubular member 17b by a conical upwardly facing funnel 17a whose upper edge is below the liquid level v and has an aperture 27 in it. it is.

The cleaned liquid drain pipe 19 in the reactor space 16 also consists of several parts; a vertical tube member 19b having an upper end above liquid level v is provided with a horizontal tube member 19c outside the reactor directly below liquid level v, while a horizontal tube member 19d extends from the lower end of the vertical tube member 19b to the interior of reactor space 16 A conical funnel 19a is provided with an upwardly facing conical funnel 19a having an orifice 27 containing a particulate material retention means. In this case, the particulate suspended material in the reactor compartments 15,16 is designated by reference numeral 18, while the sludge on the bottom 24 is designated by reference numeral 25.

The operation of the apparatus of Figure 1 is as follows: an organic liquid, such as slurry to be decomposed, is introduced through the pipe 5 into the lower portion of the reactor 1, from where the liquid flows upwardly into the reactor space 30 according to these arrows. The particulate material 18 is floated in water, on which surface microorganisms which decompose organic matter are deposited. Such a particulate biofilm carrier is a floating material having a particle size of 0 4 to 2 mm, preferably about 5 to 10 mm, of a density of 0.8 to 1.0 kg / dm ³ , preferably 0.9 to 0.95 kg / dm ³ , e.g. polystyrene foam beads, polyethylene, rubber flour, etc. applicable. In reactor 1, the liquid surface level v is free. Biocatalysts effect produced by the particulate material 18 is established in bacteria, or microorganisms in the organic pollutants ultimately methane gas (CO and partly _the -da) are reduced while maintaining the microorganism population growth (cell growth) to a minimum. The purified water from the reactor 1 is discharged through the funnel 8 and the pipe 7, respectively; the floating particulate material carrying the biofilm 18 is retained in the reactor by means of a structure 9, e.g. The formed methane gas leaves the reactor through pipe 10, through which the reactor space is vented, and the sludge collected from the bottom 2 can be removed periodically through pipe 6 (arrow b); through the openings 4 it is possible to enter the reactor interior for cleaning and maintenance purposes.

The apparatus of Figures 2 and 3 operates as follows:

Organic liquid, such as wastewater for purification, is fed through the pipe 12 into the upper portion of the sedimentation space 13 of the all reactor (tank) as shown by the arrow a. At the bottom of the settling chamber 13, some of the contamination is sedimented in the form of sludge 25 and the partially purified liquid passes through the decanter tube 14 into the lower part of the anaerobic reactor space 15 and flows upwardly through these arrows which may be identical to that described for the operation of the reactor of Figure 1. From the reactor space 15, further purified water enters the bottom of the anaerobic reactor space 16 through the hopper 17a and the transfer tube 17, from where it also flows upwardly through the floating particulate material 18 carrying the biofilm in the reactor. In reactors 15 and 16, with the formation of methane gas and, to a lesser extent, carbon dioxide, organic impurities are decomposed by microorganisms while their growth is minimal. The purified water is discharged from the reactor through the funnel 19a and the pipe 19a.

The manhole 20 serves several purposes: it allows access to the reactor interior and the installation of various structures therein. Through the orifice 20, the biofilm-containing particulate material 18 can be loaded into the reactor spaces 15, 16 and through this orifice, e.g. by sniffing - removes sediment from the sediment and 18 particulate matter, which is difficult to recover from thickened biofilm and needs regeneration; this operation is only required every few years. Finally, through the orifice 10, the resulting gases also escape.

The invention will now be described in more detail by way of example.

The reactors 15 and 16 of the reactors of Figures 2 and 3 contain 320 kg / m ³ of polystyrene beads having a density of 0.9 g / cm ³ and a particle diameter of 8 to 10 mm. Domestic wastewater containing 300 mg / l of BOl ₅ in organic wastewater is introduced into the settling basin 13. The waste water remains in the sedimentation space 13 for five days and in the anaerobic reactor spaces 15, 16 for a further 5 days. The water discharged through the 19c tube has a BODg content of only 100-120 mg / L, so purification is highly efficient and occurs in a relatively short period of time. The methane gas formed is discharged through the orifice 20. The growth of microorganisms is very small and the sludge is hardly formed. For years, the reactor has no intervention, eg. does not require regeneration.

Advantageous effects of the invention include:

The invention has a wide range of applications. Both low and high organic fluids such as sewage and livestock slurry can be cleaned. The contact bed biological reactor of the present invention can be used economically either alone or in combination with aerobic technology. The process can be carried out either in existing anaerobic reactors and leaching tanks, converting them as needed, or in new structures. In addition, the apparatus is simple in design and construction, has practically no or little internal components, requires minimal treatment, has a high purification efficiency (eg slurry treatment results in at least 80% BOD reduction and anaerobic digestion efficiency according to the invention). -40% to 60%) and maximum operational safety with no clogging. The quality of the purified water allows its good desiccation.

The invention is, of course, not limited to the above example and to the embodiments of the apparatus described on the basis of the drawings, but can be practiced in many ways within the scope of the claims.

Claims (9)

Claims A process for the anaerobic biodegradation of organic matter in a liquid, particularly for the treatment of sewage or slurry, which process is carried out in an oxygen-free environment with the help of microorganisms! decomposing the organic material into methane gas, characterized in that the decomposition is effected by passing the organic material-containing liquid through a bottom-water-floating, particulate material covered with a micro-organism bio-layer floating in the liquid. 2. Method according to claim 1, characterized in that the organic substance-containing liquid is from 0.8 to 1.0 g / cm ^3, előnyösen0,9-0,95 g / cm ³ density; On granular material having a particle diameter of 4 to 20 mm, preferably 5 to 10 mm, of 200 to 500 kg / m ³ , preferably 300 to 350 kg / m ³ , e.g. flow through polystyrene beads, polyethylene or polypropylene granules, gum flour or the like. Apparatus for carrying out the process according to claim 1 or 2, comprising a closed container having an opening-closure port, at least one reactor compartment, pipes for supplying and discharging the liquid to be treated, and a gas outlet opening, characterized in that: the reactor space (3) or reactor spaces (15, 16) having a particulate material (18) covered with a bio-layer containing microorganisms having a density less than water; a funnel (8, 17a, 19a) located below the liquid level (v), which is provided with a device (9, 27) for holding the particulate material (18) with a flange in the upper part of the reactor space (30, 15, 16); contain; and the fluid (5, 14c, 17c) feeding the fluid to be treated into the reactor space (30, 15, 16) into the lower portion of the reactor space. Apparatus according to claim 3, characterized in that the reactor space (3) is formed in a closed container having a cylindrical side wall and a conical bottom (2) and a lid (3); the liquid supply tube (5) having a downwardly tapered conical manifold (5a) at the end of the container, which is in the vertical geometric center axis (x), as well as the funnel (8) for discharging the treated liquid at the top of the container (Fig. 1). . Apparatus according to claim 4, characterized in that the deepest location of the reactor space (3) comprises a sludge outlet pipe (6) and a gas outlet pipe (10) starting from the vicinity of the highest point of the tank (Fig. 1). 6. Apparatus according to claim 3, characterized in that the settling trough (13) and a plurality of reactor compartments (15, 6) there is; the trough (12) for feeding the fluid to be treated extends into the upper portion of the settling space (13); the nlepítőteret dekantálócső (l ^z l) connects the first reaktortérrel (15) having a tubular member in the first reactor (15) (14c) opens into this reactor (15) at the bottom; the first reactor compartment (15) being connected to the second reactor compartment (16) by a conduit (17) having a funnel (17a) provided with a particulate retention device (27) in the first reactor compartment (15), the second reactor compartment (16) and its existing tubular member (17e) extends to the bottom of this reactor space (16); and, in the direction of the flow of the liquid, out of the last teacup compartment (16) at the top here, in the funnel (19a) ending in a funnel (19a) with a particulate retention device (27). Apparatus according to Claim 6, characterized in that the reactor (11) has a cylindrical vessel in which the settling chamber (13) is semicircular and the reactors (15, 16) are fourth (figure 3). 8. Referring to FIGS. Apparatus according to any preceding claim, characterized in that the reactor (30) or -terekben (15, 16) is 0.8 to 1.0 g / cm ^3, preferably 0.9 to 0.95 g / cm ³ density, 4- 20 mm, preferably 5-10 mm grain diameter, 200-500 kg / in ^3, preferably 300-350 kg / m ³ of granular material floating. For example, pre-expanded polystyrene beads, polyethylene or polypropylene granules, or rubber mills. 9. Apparatus according to any one of claims 1 to 5, characterized in that the funnel (8, 17a, 19a) has a particle retention structure (9, 27), a mesh or grid with a hole size smaller than the grain diameter of the particulate material (18).