CS214897B2 - Method of evaluation of the mud containing organic impurities and facility for executing the same - Google Patents

Abstract

A process for the utilization of anaerobic digested sewage sludge which comprises: (a) heating the digested sewage sludge to at least 80 DEG C and then optionally cooling it from 80 to 40 DEG C; (b) separating the heat treated digested sewage sludge, optionally in the presence of a coagulant, to give a concentrate and a supernatant; (c) preparing a culture medium by adding to the supernatant a C1-C3 alcohol and a nitrogen-containing inorganic salt and, optionally, one or more water-soluble vitamin precursors or growth factors; (d) inoculating the culture medium with anaerobic digested sewage sludge; (e) anaerobically fermenting the inoculated culture medium at from 26 to 38 DEG C; (f) separating the biomass from the fermentation liquid formed during the fermentation. e

Description

SUMMARY OF THE INVENTION The present invention further provides a method and apparatus for disposing of sludge in urban ((municipal) wastewater treatment) as a byproduct, the present invention further comprising a nutrient solution (supernatant) as well as a process for product discharging. containing the bacterial protein and vitamins obtainable by using this nutrient solution.

The solution of urban wastewater treatment and the destruction of by-products (© Wastewater treatment and highly polluting environments, or their recovery by any means of recovery) has been required for a long time. on environmental protection requirements and reducing wastewater treatment costs.

In order to stabilize the unstable by-products, which are lost in the purification of urban water, as a cathode-containing liquid obtained from the water. The primary sludge, additionally sludge sediment, obtained after biological treatment, or a mixture of both, raw sludge, is "most commonly used. rotting by anaerobic fermentation. On. ·. Lementation is most often followed by an additional fermentation tank, which essentially forces the sedimentation (secondary fermentation tank), and an already digested sewage sludge emerges from the additional digester tank. Numerous methods for removing or recovering digested sludge are already known. The first step - processing is to concentrate the sludge, the most promising method of which is to deposit in the sludge fields, in itself a considerably uneconomical process with a large space requirement and a high degree of space. degrading low productivity, another method is machine-made dewatering and subsequent destruction by incineration. Incineration is an energy-intensive process and valuable substances contained in sludge cannot be recovered.

The newer method compensates for the valorisation of valuable components present in the sludge with the inefficiency of sludge removal. Among these new methods, mention should be made of the recovery of incineration ash, the drying of dewatered sludge instead of incineration, the spreading of dried sludge, carried out directly or mixed with some other substance, field, composting, etc. the fact that its value is not in any real relation to labor and transport costs. A further drawback - that is, the biodegradable sludge substances digested in this way are only recovered to a small extent, in cattle breeding, and only indirectly, with a low degree of efficiency.

In another treatment group, one sludge component is obtained. An example is - obtaining extremely valuable -vitaminu _J2 B - In this method -působí -vsak processing agent remaining unchangeable trouble.

In the method of DOS 2 504 412, the activated sludge is partially stabilized by an -aerobic-followed by aerobic degradation. The digested sludge falling off as the final product is used for fertilization after drying. The advantage of partial -aerobic digestion is the short residence time in large digesters, whereby the flammable gases produced by the condition of anaerobic decay are largely released during this time and the rapid aerobic step, possibly resulting in partial dewatering, provides an easy to use product .

However, only soil improvers can be obtained with this method.

According to the solution described in Hungarian Patent No. -158,172, semicontinuous digestion of crude sludge by means of specific nutrients is controlled to produce equally favorable microorganisms suitable for the production of vitamin Bj2 and other microorganisms living in digestion vats. conditions. In this way, the production of vitamin Bi2 and the increase in the amount of biomass occur in the digestion vats. Additive biomass results in a greater amount of digested sludge, which due to its vitamin content is suitable as an additive to feed, and its protein content is not greater than the protein content of the digested sludge in a conventional manner.

Natural bacterial flora - from anaerobic digestion of sludge from wastewater treatment - can enrich species suitable for the production of vitamin Bn. and proteins, for example according to Hungarian Patent Specification No. 153 740. According to this method, bacterial flora from digested kata, further cultivated on suitable nutrient media, is used for the production of vitamins and - protein, using the sludge itself with cultivation bacteria is unnecessary. For the issues outlined in the introduction with respect to the use of wastewater by-products, the present invention provides no solution.

The solution described in Swedish patent 417 540 is directed to the use of sewage sludge for feed purposes. According to this solution, the recovered sludge alone or mixed with the additives is fed to a continuously operating extruder, heated briefly to a temperature of 105-160 ° C and then suddenly expanded and finally the product is air dried. Expansion causes disinfection of the product within seconds. By technical expansion, a product suitable for feed purposes is produced directly from sludge substances. Taking into account the fact that the sludge itself contains relatively ballast substances and animal organisms of a higher degree of economically unusable other substances with a relatively small amount of protein 214897, the potential feeding potentials found in this sludge are adequately utilized by this method. .

It is an object of the present invention to provide a solution for the treatment of sludge containing organic impurities, which falls especially during urban (municipal) wastewater treatment, by means of which the sludge is treated to its fullest extent so that, for example, whereas, as a result of the processing, valuable organic and inorganic substances - in particular proteins, vitamins and metals - present in the sludge would be available in the form of health and hygiene requirements for fully corresponding end products, suitable immediately for feed purposes.

The invention is based on the discovery that, in the case of. when the appropriately heat-treated and anaerobically digested sludge is divided into a concentrate and a supernatant, the latter is surprisingly and surprisingly suitable for the cultivation (multiplication) of microorganisms and, within this selective cultivation of the bacterial flora utilizing methanol and thus for producing products (biomass) ), rich in proteins. Heat treatment destroys pathogenic bacteria and at the same time sterilizes the sludge, while large-scale. the components of the heat-treated supernatant are more suitable for enzymatic degradation, the protein fermentation makes the end product composition more constant, and more suitable for feed purposes, and the separation of sludge phases - into supernatant and concentrate - may also be more advantageous. Methanol added to the heat-treated culture supernatant thus plays approximately the role of a 'selective sterilizing agent', as it prevents the proliferation of pathogenic bacteria. Finally, by drying the biomass, it stabilizes, in other words, preventing its decomposition - which would otherwise occur extremely quickly.

The basis of the invention is furthermore the fact that the equipment required for sludge removal and recovery can be constructed from building blocks known in the art, but for the purpose of using suitably selected tanks, pumps, apparatuses, equipment, etc. in the field of waste water treatment, both in the fermentation area, in order to enable, as a result of their particular combination and joint use, the complicated working processes of sludge treatment into sterile nutrients in a single rational technological sequence and that the whole plant can be set up such as waste water treatment plants - or in its immediate vicinity.

Based on this knowledge, the task was solved by means of a method used for the evaluation of digested sludge and a device for carrying out this method.

The following workflows are used during the process in the following order:

(a) the digested sludge is heated to a temperature. at least 80 ° C,. . but. preferably to a temperature of 100 to 150 ° C. a. then. during · heat treatment. optionally cooled to 80 to 40 degrees C;

b) the digested and heat-treated sludge is optionally present. the coagulating agent is divided into. a slurry concentrate and supernatant;

(c) alcohol 1 to 10 is added to the supernatant. 3 carbon atoms, preferably methanol; at least one inorganic salt containing. nitrogen, optionally one. or more water-soluble. vitamins,. as well as the bio-substance (s), and thus. manufactures. nutrient medium;

d) the culture medium is preferably. anaerobically inoculate digested sludge;

(e) the inoculated broth is fermented anaerobically at a temperature of 26 to 33 ° C; .

f) biomass is separated from the fermentation liquid formed during fermentation. According to a further aspect of the invention, it is provided. biomass. . - preferably sprayed - dried.

The apparatus consists in having a heat exchanger suitable for heating and cooling the digested sludge, a device for separating the digested and heat treated sludge into supernatant and sludge concentrate, a tank used for the production of nutrient broth, a fermentation tank suitable for fermentation of nutrient soil as well. i separator,. serving to separate biomass from the fermentation liquid formed in the fermentation tank.

The present invention further comprises:

A nutrient solution (supernatant) suitable for the cultivation of microorganisms and obtained by heat treatment. treating and separating the digested sludge, the solution of which is characterized by:

(a) its nitrogen content ratio. v. inorganic and organic substances is 1: 1 to 10: 1,

(b) its acidity, expressed in. formic acid, is between 500 and 5000 mg / l.

2. Protein and vitamin rich product, preferably suitable for feed purposes, with a nutrient solution (supernatant) obtained by heat treatment and enrichment of digested sludge. nutrients, obtained by anaerobic fermentation, characterized by its

(a) Crude protein content> 50% w / w

(b) a total water-soluble vitamin content> 1000 y / g.

21489 7

Advantageous effects associated with the invention are as follows:

In accordance with the invention, the wastewater sludge material is processed and recovered for an extremely valuable product having a high content of protein and vitamins and / or metals, and usable for feed purposes, the storage, storage or / in any other way the removal was - the most significant • burden · · waste water treatment - and - last but not least - the unsolvable task of waste water treatment. In this way, it has been possible to eliminate the severe hygiene problems and environmental protection problems by making sterile the unused and unprofitable protein sources and vitemilins at the same time. - for (feed-purposes - with · excellent-matching-product), ie - not only - costs - for - wastewater treatment are eliminated, but also substantial new values are generated. After-treatment of the sludge, there is no additional harmful product, and another advantage is that it increases even further as a result of fermentation of the biogas-producing supernatant. high energy content.

The composition of the main feed product suitable for feed purposes produced by the process according to the invention (see further examples -1, 5, 6 and 7j in Table 1 compared to the composition of the digested sludge) The data illustrates well the significance of the result achieved by the invention.

The invention will now be described in detail with reference to the accompanying drawings and examples. The drawings show the apparatus used for carrying out the method, if necessary, for balancing ^! diagram.

In the drawings, FIG. 1 shows an example of a preferred embodiment of the apparatus in a schematic side view and FIG. 2 shows a balance diagram pertaining to a specific example of the method according to the invention.

Na -obr. 1 - there are - connecting - individual parts - devices, or into these outlets, or - out of these outlets, - and arrows showing - the flow of material - are drawn - whereby - it is possible - well - to follow the technological processes taking place in -equipment.

The wastewater treatment plant (not shown in detail) comprises a digestion chamber 1 into which the raw sludge 2 is introduced and from which a pipe 3 is provided for the further conduction of the biogas forming - during the anaerobic digestion process, into a (not shown) collecting tank.

The firing chamber 1 is connected via a line 9 comprising a centrifugal pump 5 with a storage tank (tank) 7, which is connected via a line -8- ^! to the heat exchanger 9. The heat exchanger 9 comprises exchanger units 11, 12 of which the exchanger unit 12 heats the digested liquor and the exchanger unit 11 cools it, while - in accordance with the heat exchanger unit 12 joins the steam conduit 13. The heat exchanger units 11 and 12 are connected together by a conduit 14 and 15, the conduit 16 connecting the exchanger unit 11 to the gravity sedimentation tank 17 into which the paddle stirrer 17a extends. similar equipment.

T a b at 1 k a - 1 digested main product produced by the sludge according to the example

. 1 5 .6 7 total dry matter g / 100 -g fermentation juice 10.2 2) 5 2.56 2.40 3.38 crude protein -in% - dry matter 17.7 69 71 '63, 5 digestible protein - in crude protein ,8 24.8 53 '56 51 58 vitamins: -gamma / g Vitamin ® | gamma / g 0.60 17.2 8.2 22.0 1-5,5 vitamin B2 gamma / g 1.42 150.0 124.0 210.0 130.0 Vitamin B ₆ gamma / g 3.45 187.0 130.0 150.0 850.0 vitamin gamma / g 5.40 85.0 35.0 55.0 38.0 -nicotinic acid-gamma / g 2,0 160, 0 120.0 167.0 125.0 chloride, .gamma.-g / g 0,098. 100.0 985.0 1180.0 1510.0 gamma / g 0.51 12.5 25-0 290.0 17-0 pantothenic acid gamma / g 14.5 125.0 98.0 374.0 285.0

The sedimentation tank 17 is connected via a line 19 comprising a centrifugal pump 18 to the reagent dissolution device (duplicator) in which the water inflow 21 flows.

At the bottom of the sedimentation tank 17, the conduit 22 to which the centrifugal pump 23 is connected is branched off. In front of the centrifugal pump 23, a tube 24 extends from the top of the sedimentation tank 17 into the pipe 22 via a plurality of branches. The pressure line 24a extending from the centrifugal pump 23 opens into a decanter centrifuge 28. From the line 24, a line 25 is branched off the centrifuge 28 and flows into a reservoir 26 for collecting the nutrient solution supernatant (see FIG. 1, lower left). Two lines extend from the decanter centrifuge 28, the line 27 opens into the line 25, the line 28a, on the other hand, connecting - the centrifuge - 28 to the concentrate container 29; in the concentrate container 29 there is a stirring paddle 29a or the like.

The concentrate reservoir 29 is connected via a conduit 31 comprising a centrifugal pump 30 to a rotary drying chamber 32 below which the outlet opening of the homogenizer 33 is arranged and below the bagging scale 34.

The reservoir 26 for the collection of the supernatant and for the preparation of the nutrient medium is connected via a conduit 37 comprising a centrifugal pump 36 to a nutrient solution reservoir arranged below the floor level, into the reservoir -35 the steam conduit 38 and water supply 39.

The reservoir 28 is connected via a line 42 to a storage tank 40 containing methanol needed for the preparation of the nutrient medium, and a self-priming pump 41 is built into the line 42 (for example, a self-priming methanol pump of the SIHI type). A mixing paddle 26a 'or a similar device is disposed in the reservoir 26.

The reservoir 26 is connected via a conduit 44 comprising a centrifugal pump 43 to a fermenter 45 into which - an orifice - a conduit -45a serving for feeding with a vaccine - preferably a sludge digested in an anaerobic manner. The outgoing conduit 46 serves to evacuate the biogas, a conduit 48 comprising a centrifugal pump 47 and serving to further convey the fermentation juice to the second storage tank 49, in which a mixing vane 49a or the like is arranged. A conduit 52 comprising a centrifugal pump 51 is used to further convey the fermentation juice from the reservoir 49 to the separator 50. Biomass passes from the separator 50 through the conduit 54 to the storage tank 53, the conduit 55 serving to return the supernatant excreted in the separator to the waste treatment system. water.

The line 57, emerging from the tank 53 and containing the centrifugal pump 56, opens into the top of the powder-drying drier 58. Below the powder-drying drier 58 is a homogenizer 59 and below this a bagging scale 60.

K - devices belong - logically arranged - in a corresponding number - in known numbers - slide valves - - or other - - devices whose representation has been omitted for clarity; however, their location - and the destination - is obvious to the skilled person.

By means of the device according to FIG.

The sludge - - digested in the digestion chamber 1 - anaerobic access - air access - at a temperature of 30-35 ° C is transported - via a centrifugal pump 5 to a storage tank 7 and from there by a centrifugal pump 10 - - into the heat exchanger 9.

The capacity of the digestion chamber 1 - corresponds, depending on the purpose for which it is to be used, about ten times the volume of the raw - sludge falling off daily - during the waste water treatment. Prior to the feed of the raw sludge, the amount of the digested sludge equal to the amount of the raw sludge supplied is always taken from the digester chamber. These processes can be carried out in the same way periodically, semi-continuously or continuously. The term - semi-continuous operation - means that the supply - and - the supply is carried out daily - once or - every 8 to 12 hours.

If - if necessary - the temperature is maintained in the digester 1 by cooling or heating - within the specified temperature range of - 30 to 35 ° C. The preferred pH value of the digestion is 7 to 8; - in the case of acidity, it can be regulated by the addition of lye, preferably lime milk.

The digested sludge is passed through the heat exchanger units 11 - a - 12 and is heated - at least at least - to - 80 ° C, - preferably to a temperature of 100 to 150 - ° C, - - - and thereafter - - it is cooled, preferably at a temperature of - 40 - to - 80 - ° C, and - it is transported to a sedimentation tank 17. This - 'heat treatment' - destroys the flora of the digested sludge microorganisms. - including pathogenic bacteria, ie - sludge - se - stasis. Another result of the heat treatment is that the sludge gets to a more favorable state for the concentration process and the nutrient solution (supernatant) to the favor ^; state - for further processing. In the area of - heating, the lower temperature values are the longer heating times, - higher temperatures the shorter heating times.

In the sedimentation tank 17, coagulation agents - for example, inorganic - can be used to re-cool - sludge containing entrained solid particles, - partially coagulated - during heat treatment, for easier - - separation of these particles - with vigorous - mixing of the tank contents or organic electrolytes, for example aluminum sulfate, iron sulfate or polyacrylates, polyacrylamides. Possible coagulating agents may also be - colloids exhibiting amphoteric behavior (e.g. natural adhesives) or organic non-electrolytes (e.g. starches) - [Flokkungsmittel in Wasseraufbereitungstechnik, Chem.

214697

Rdsch. (Solothurnj 2n _t 677-Q7lą77 j.

The basic consideration in the choice of a coagulating agent is that this use must not interfere with the use of the final product as feedstuff, so that for example, IC Ciearfiook AN 10 (manufactured by Industriai Chemicais and Equipment Inc) can be used as a coagulating agent. Preferably, the surfactant is fed to the sludge in an aqueous solution, which is then allowed to settle for several hours, preferably 2 to 6, and it is preferable to use aluminum sulphate as a coagulating agent. The addition of a coagulating agent can also be omitted in certain cases and sedimentation in the tank can also be carried out without it.

From the bottom of the sedimentation tank 17 sedimented sludge is collected there and in the same way from the upper part of the sedimentation tank 17 the nutrient solution is removed by means of a centrifugal pump 23, which must be logically actuated by a slide valve (not shown). The solution (the supernatant is then passed through line 25 to the reservoir 26, the sludge is passed through line 24a to the decanter centrifuge 28.

From the sludge, as a result of the described decantation process with a concentration degree of activity of 0.90 to 0.95, a concentrate in an amount of about 30 to 50% by volume of a nutrient solution (supernatant in an amount of 50 to 70% by volume; the dry matter content of the sludge is about 12 to 18%, the dry matter content of the nutrient solution is 0.5 to 1.0 why.

In the centrifuge 28, the concentrate is further dewatered, during which 30 to 50% by volume of the concentrate and another nutrient solution are obtained. The dry matter content of this concentrate is from 30 to 40 W.

The concentrate having this high solids content is then passed through a conduit to the concentrate reservoir and from there to the rotary drying chamber 32 by means of a centrifugal pump. It is dried here and / or until the organic substances disappear. Annealing. Drying is carried out at a maximum temperature of 150 ° C, because using higher temperatures breaks down valuable proteins. Only the dried product is referred to as by-product I, the annealed product is referred to as by-product II. Both products are valuable: the first one has a more significant protein content, the second one has a more significant metal content, and as a result these products can be used alone or together and / or mixed with other substances - for example the main product obtained by the process - in animal feed. By means of the homogenizer 33 and the bagging scales 34, mixing and dosing processes can be carried out precisely.

The resulting nutrient solution (supernatant resulting from decantation by centrifuge 28) is fed via line 27 to the same line 25, which also feeds the nutrient solution (supernatant obtained in sedimentation tank 17, into reservoir 26. · From the nutrient solution (supernatant obtained from of the two sources mentioned above, in a container 26, a culture medium suitable for fermentation is produced by adding to the nutrient solution (supernatant from the tank · 35 as a nitrogen source a solution of a nutrient salt, preferably a solution of at least one salt of the largest parts of inorganic ammonium salt, as carbon source, a C 1 -C 3 alcohol, preferably methanol, fed from tank 40 via a self-priming pump 41 via line 42 as well as by line 37 known and commonly used in fermentation for biofuels. preferably, use of ammonium bicarbonate, ammonium hydrogen phosphate or nitrate Molasses, glycine, yeast - preferably brewer's yeast hydrolyzate - magnesium chloride, etc. may be suitable as a bio-substance. If, during fermentation, not only the high protein content of the biomass is taken into account, but also well known water-soluble vitamins precursors may be added to the nutrient solution to produce a main product, rich in water-soluble vitamins and suitable for feed purposes. Such precursors may be, for example, pimelic acid, nicotinic acid, and the like.

At the same time, the presence of methanol in the nutrient medium in relation to pathogenic bacteria plays the role of a selective sterilizing agent as it prevents - along with the multiplication of numerous other strains of bacteria - the multiplication of pathogenic bacteria.

The nutrient medium produced in the container 26 - also by means of a stirring blade 26a - is conveyed by means of a centrifugal pump 43 via a line 44 to a fermenter 45 to which the inoculum is also fed - preferably an anaerobically digested sludge taken from the digester 1 1/10 to 1/20 of the useful volume of the fermenter 45 through line 45a. The capacity of the fermenter 45 is appropriately intended to be equal to that of the digester 1. Here, the inoculated nutrient broth is fermented in an anaerobic manner in a manner known per se and the resulting biogas is fed via line 46 to a gas tank (not shown). After the fermenter 45 has been filled, the microflora required for the production of the cellular protein is formed (within about 5-10 days), after which the fermentation is carried out continuously or semi-continuously. In the case of semi-continuous fermentation, about 10% vol. The same amount of nutrient medium is fed to the fermenter 45 at the same time as the centrifugal pump 47 into the storage tank 49 and at the same time - or with some delay.

The fermentation liquid is fed from the storage tank 49. to a separator 50 where biomass is then separated from the fermentation liquid. As a result of the separation process, about 80 to 90% by volume of the nutrient solution, the supernatant, is produced, which is then fed back via line 55 to a biological waste water treatment system. This may be all the more so because the BOI5 value after separation of the biomass remaining on the cell lean fermentation liquid is 120-150, and therefore the biological treatment of the waste water is almost unloaded. BOI5 - the concentration of nutrient solutions remaining after concentration used in conventional wastewater treatment by centrifugation is so high that this must be taken into account when determining the dimensions of biological treatment systems.

The extract obtained by separating the fermentation liquid-biomass, which is about 10 to 20% by volume of the fermentation liquid collected, is conveyed to the storage tank 53 and from there via a centrifugal pump 56 via line 57 is pushed into a known powder dryer 58. Here, as a result of the drying process performed, the main product of the process of the invention is comprised of about 70% crude protein and a considerable amount of water-soluble vitamins. It is necessary to emphasize the stabilizing effect associated with drying and acting on biomass, in order to prevent the decomposition of otherwise extremely perishable biomass, in other words, the so-called biomass is preserved and a condition suitable for packaging, transport and storage and dosing.

The invention will now be described in detail by way of examples, in which the names and designations of FIG. 1 are used logically.

Example 1

The balance diagram of the example is shown in Fig. 2.

In a digester 1 having a useful capacity of 300 m ^{3 of} raw sludge. The digestion is carried out anaerobically at a temperature of 30 ° C to 35 ° C and a pH value of 7 to 8. The digested sludge contains a significant amount of organic and inorganic substances, a total dry matter content of 7% by weight.

m3 of daily digested sludge is passed through a heat exchanger 9 and subjected to a heat treatment in which it is first heated at 100 degrees Celsius for 15 minutes and then cooled back to 60 ° C. The digested heat treated sludge is fed to the sedimentation tank 17 and 60 kg of aluminum sulphate Al ₂ (SO ₄ ) 3 are added thereto. . 18 H ₂ O dissolved in 300 L of water. The thus formed precipitate adheres or coagulates the suspended solid particles of the heat-treated digested sludge. In the above-mentioned manner, the digested sludge is sedimented for four hours, so that 60% of the total volume can be decanted as a nutrient solution (supernatant) (see FIG. 2 below). During decantation, 18 m ^{3 of} nutrient solution (supernatant) containing 0.54 ·% by weight of dissolved solids (dry matter = 0.1 · t) and 12 m ^{3 of} concentrate containing 16.7 ·% by weight of solids ( dry matter = 2.0 ie.

The nutrient solution (supernatant) is pumped into a reservoir 26 of 50 m ³ . The concentrate is fed to a centrifuge 28, followed by further dewatering, to obtain 5.4 m ^{3 of a} concentrate having a solids content of 35% by weight (dry matter = 1.9. T) and 6.58 m3 of nutrient solution. [Supernatant] with a dissolved solids content of 1.58 ·%! % (dry matter = 0.1 t), which are also conveyed to the aforementioned container 26 having a capacity of 50 m ³ .

From the digested sludge treated with aluminum sulphate, as a result of both separations (sedimentation and centrifugation), 24.6 m ^{3 of} nutrient solution (supernatant) containing 0.85% by weight of dissolved solids (dry matter = 0, 2 t) and a concentrate having a solids content of 35% by weight (dry matter = 1.9 tonnes), the last being dried in a rotatable drying chamber 32 at a temperature controllable at 140 degrees Celsius. . · · 1.77 t of 'by-product I' containing 'ΊΟ why. water. ί · '· ^: >. ·

The dry matter content of 'by-product I' has the following composition:

total organic substances 59; % Crude crude protein 18% ash containing metal oxides 41 ·% acid-soluble Fe ²⁺ 'content 2,1' · · '% acid-soluble Cu ²⁺ content 0,18 ·%

Zn ²⁺ 0.25%

Mn ²⁺ 0.36% o

Mg ²⁺ 0,30%

Co ²⁺ 0,10%

Ca ²⁺ 3.2 ·% all P 2.6%

To the nutrient solution (supernatant) (24.6 m ³ ) combined in tank 26, add the following substances, dissolved in 5.4 m ^{3 of} water:

300 l of methanol kg of ammonium bicarbonate kg of ammonium hydrogen phosphate kg of glycine kg of molasses kg of brewer's yeast (hydrolyzate)

The nutrient solution (supernatant) and the aforementioned solution are mixed in a tank of 26 with a capacity of 50 m ³ to obtain a fermentable broth which is conveyed into an empty tank having a useful capacity of 300 m ^{3 of} fermenter 45 while has previously been fed from freshly digested sludge · to a conventional 30 m3 waste water treatment plant. The temperature of the fer214197 mentor 45 is set at 32 ° C and maintained at this temperature, and the contents are stirred for 6 hours.

As a one-time start-up of the fermenter 45, the feeding of the nutrient solution (supernatant) supplemented with the calculated substances and 30 m ^{3 of the} digested waste water sludge as inoculum is carried out for five days.

From day 6, as described above, the fermenter 45 commissioned is operated semi-continuously, by withdrawing 30 m ^{3 of} fermentation liquid prior to feeding and then adding 24.6 m ^{3 of} nutrient solution to which they were added the following substances dissolved in 5,4 m3 of water (see also Figure 2, right side):

1500 L of methanol

180 kg of ammonium bicarbonate

- kg of ammonium hydrophosphate kg of glycine kg of molasses kg of magnesium chloride kg of brewer's yeast - (hydro-lysate)

Furthermore, the fermentation is carried out semicontinuously, in periods of 24 hours after collection of 30 m 3 of fermentation liquid and addition of 30 m ^{3 of} nutrient medium (dilution rate 0.1 day ^-1 ). 30 m ^{3 of} the fermentation liquid collected contains 2.5% by weight of total dry matter (dry matter + 750 kg). - Suftna - contains a number of bacteria, which sweep through the action of methanol and other substances (biomass). The biomass is separated separably from the fermentation liquid. From 30 m ^{3 of} fermentation liquid, 2.23 m ^{3 of} concentrate with 30% by weight of dry matter (dry matter + - 670 kg) are obtained and

27.7 - m ^{3 of} nutrient solution (supernatant) with 0.3% by weight, dissolved solids (dry matter +, -f- 80 kg) and this nutrient solution is returned to the biological treatment system of the urban wastewater treatment plant.

The biomass is dried in a powder dryer 58 and the powdered - "main product" with a moisture content of 10% is in accordance with 627 kg.

Based on the dry matter, the composition of '

product ": crude protein: 69% Vitamins: vitamin Bi 17.2 y / g vitamin B ₂ 150.0 y / g vitamin B _e 187.0 y / g vitamin B12 85.0 - y / g nicotinic acid 160.0 y / g Choline chloride 1100.0 y / g panthotenic acid 125.0 y / g

m ^{3 of} digested sludge, 7%, 2.1 t, 104 heat treatment: heating - cooling, 105 300 liters of 20% aluminum sulphate solution, 106 mixing, sedimentation, decantation, 107 12 m ^{3 of} concentrate, 16.7 -%, 2 t, 108 18 m3 nutrient ^Ho solution, 0.54%, 0.1 t 109 centrifuge 110 54.2 Ni3 - concentrate 35%, 1.9 t 111 6.58 m3 nutrient solution, 1 53%, 0.1 t, 112 drying, 113 3.33 m ^{3 of} water, 114 10% powder loss, 115 24.6 m ^{3 of} combined nutrient solutions, 0.85%, 0.2 t, 116 to 300 m3 fermentor, 117 homogenization, 118 5% powder loss, 119 24.6 m ³ nutrient solution, 0.85 why., 0.2 t, 120 nutrient dissolved in 5.4 m ³ water ', and methanol, 121 secondary product I 1.77 t, -90%, 122 300 m ^{3 of} fermenter, 123 annealing plants, 124 30 m ^{3 of} fermentation liquid, 2.5 ·%), 0.75 t, 125 0.72 m ^{3 of} organic substances, -burnt , 126 by-product II, 1.05 t, 127 separation, 128 27.7 m3 nutrient solution (0.3%, 0.08 t), 129 2.23 m3 concentrate, 30%, 0.67 t , 130 drying, 131 1.49 m 3 of water, 132 10% powder loss, 133 homogenization, 134 recovered in biological treatment, 135 5% powder loss and -136 main product 0.63 t, 90 ·%.

Example 1 -and d 2

In each respect, the procedure of Example 1 was followed, except that the digested sludge fed to the heat exchanger was maintained at 120 ° C for 5 minutes. The amount and composition of the obtained "by-product" and "main product" correspond to the quantity shown in Example 1.

Example 3

In all respects, the procedure of Example 1 is followed, except that 30 kg of IVC Clearfloo ANlo (anion-containing organic, easily decomposing polyelectrolyte) dissolved in 3000 liters of water is added to coagulate the heat-treated digested sludge - (Industrial Chemicals product) and - Equipment Inc (AG., Vienna).

Quantity of products obtained:

'By-product I' 1,881 'Main product' 0,711

Product composition - (dry matter): 'by-product I' of all organic substances: 52% 'of which crude protein 21,0% metal oxides, contained in ash content of water-soluble cations:

Fe ²⁺ 2.5%

Cu2 + 0.09%

Zn ²⁺ 0,31%

Mn ²⁺ 0.29%

Co ²⁺ 0.09%

Ca ²⁺ 3.5% all P 3.0%

Giant. 2 shows the balance diagram of this example, where 101 denotes 30 m3 of raw sludge, 102 digester 300 m ³ , 103

214 * 97

The composition of the "main product" agrees with the composition given in Example 1.

Example 1 a d 4

In each respect, the procedure of Example 1 was followed, but with the change that only 600 liters of methanol were added to the nutrient broth obtained daily by semi-continuous fermentation instead of 1500 liters of methanol. The amount and composition of the 'by-product Г' are the same as those in Example 1.

Main Product Quantity 64%

Vitamins:

vitamin B, 12 y / g vitamin B ₂ 53 y / g vitamin Be 154 y / g nicotinic acid 112,0 y / g choline chloride 34,0 y / g biotin 3,2 y / g piutolh ^ tf ^ iu ^ 63., 15 y / g

Example 5

Up to the production of "by-product I", the principles of Example 1 are followed in each respect. To produce the "main product", 180 kg of ammonium bicarbonate, 120 kg of ammonium bicarbonate per day are added to the broth obtained by fermentation instead of Example 1. and 120 kg of ammonium nitrate. Example 1 was followed.

The amount and composition of 'by-product I' are consistent with the data in Example 1 Quantity of 'main product' of composition: Crude protein 1050 kg 71% ' vitamins: vitamin Bt vitamin B2 vitamin B {i vitamin B _n nicotinic acid choline chloride biotin panlCottnic acid 8.2 y / g 124.3 y / g 130.0 y / g 35.0 y / g 120.0 y / g 985.0 y / g 25.0 y / g 98.0 y / g Example 6

Until the production of "by-product I", the procedure is carried out in every respect as in Example 1. To produce the "main product", 2 kg of pimelic acid as precursor is added daily to the culture broth obtained by fermentation. The procedure was as described in Example 1.

The quantity and composition of 'by-product I' correspond to the data given in the example

1.

Quantity of 'main product': 765 kg

Crude protein 64% vitamins:

Vitamin B, 22,0 Vitamin B ₂ 210,0y / g Vitamin B ₆ 150,1 γΐ0 Vitamin Bi 2 55, Оу / 0 Mktotnovic acid 167,1у / 0 Chlorine chloride 1180,1 y / 0 Biotin 250,00 / P »nth (rten (W 374.3 // 0)

Example 1 a d 7

It proceeds until the production of "by-product I" as described in Example 1.

For the production of the 'main product', 5 kg 'of nicotinic acid is added as a precursor to the nutrient broth. The procedure is as described in Example 1.

The amount and composition of "by-product I" corresponds to the data given in Example 1.

685 kg of 'main product' ingredients: · raw protein: 63,5% vitamins:

vitamin B, 15.5 y / g vitamin Во 13O, 1y / 0 vitamin Bti 850.8 y ^ vitamin B _u 38.0 nicotinic acid 125.05,, 0 choline chloride 1510.5y / 0 biotin 17.0 // Pantothenic acid 285.2 y / 0

Example 1 a d 8

The digestion, heat treatment and separation of the digested sludge are carried out as described in Example 1. The concentrate is annealed at a temperature of 500 ° C (see lower left part of the balance diagram of Fig. 0).

In this way a 'by-product' II 'is obtained. The production of the "main product" is carried out in the same way as in Example 1. The amount and composition of the "main product" are consistent with the data given in Example 1.

Quantity of 'by-product II': 1,5 t

Ingredients: organic matter content: 0.0% acid-soluble cation content:

Fe0 + 5.12%

Cu2 + 0.43%

Zn2 + 0.61%

Mn0 + 0.87%

Co2 + '0.24%

Ca2 + 7.8%.

all P 5,2%

215 8 9 7

Naturally, the invention is not limited to the examples described in detail, or the embodiment described and illustrated

Claims (23)

SUBJECT A process for the recovery of sludge containing organic impurities, in particular falling off as a by-product of urban wastewater treatment, and digested by an anaerobic process, characterized in that the digested sludge is heat treated by heating to a temperature of at least 80 ° C, preferably 100 to 150 degrees Celsius, then optionally cooling to 100 ° C. 80 ° C to 40 ° C, then the heat-treated digested sludge, optionally in the presence. coagulating agent, divided into a concentrate. 'sludge'. and nutrient ^: 'solution' and addition of alcohol. . 1 'to 3 carbon atoms, _s',' vý'hodou: methanol. at least . inorganic: salts containing nitrogen and. optionally a vitamin B precursor or vitamins. B,. . as well as trioles to the nutrient solution, a nutrient broth is formed which is inoculated with sludge, preferably in an anaerobic digested manner, and the seeded broth is fermented anaerobically at a temperature. 26 to 38 ° C and from the fermentation liquid formed during. the biomass is separated from the fermentation and then dried. 2. The process according to claim 1, wherein: the biomass is preferably spray dried. 3. The method according to claim 1, characterized in that it is as. the coagulating agent uses inorganic or organic electrolytes, colloids exhibiting amphoteric behavior, or organic non-electrolytes. 4. The process of claim 1 wherein the inorganic coagulant is aluminum sulfate. A process according to claim 1, characterized in that ammonium bicarbonate and / or ammonium hydrogen phosphate and / or ammonium nitrate is used as the nitrogen-containing inorganic salt. 6. The method of claim 1, wherein the precursor of the water-soluble vitamins is pimelic acid. 7. The method of claim 1, wherein the water-soluble vitamin precursor is nicotinic acid. 8. The method of claim 1 wherein the drying of the concentrated biomass is carried out up to a moisture content of at least 10 why. 9. Process according to claim 1, characterized in that, in the case of a semi-continuous sequence of operations, the nutrient-enriched nutrient solution is fermented in a fermenter with a capacity at least equal to five times, preferably ten times, its daily production. 10. An apparatus for the recovery of sludge containing organic impurities, in particular falling off as a by-product of urban wastewater treatment and digested equipment, but. can . . within the scope of patent protection to carry out 'in many others'. embodiments. OF THE INVENTION. anaerobic '. method according to 'Claim 1: wherein:: the ^J by "' comprises a heat exchanger (9) of heat, arranged 'to' heating and cooling the digested 'fcálu, spójerfý · leadership' device fart ··: dividing the 'heat treated: digested sludge, and the' reservoir '(26),' connected 'by the conduit (44) to the fermenter (45), and the separator (50). Apparatus according to claim 10, characterized in that a storage tank (7) is arranged upstream of the heat exchanger (9), arranged to store the digested sludge from the waste water treatment plant. Device according to claim 10 or 11, characterized in that the heat exchanger (9) comprises at least two heat exchanger units, one of which is arranged as a cooling exchanger unit (11) and the other as a heating exchanger unit (12). Apparatus according to claim 12, characterized in that the heat exchanger units (11: and 12) are designed as open and closed spiral tube heat exchangers. 14. The apparatus of any one of items 10 to 10 13, characterized in that the device arranged for separating the digested sludge into a nutrient solution and the sludge concentrate is a decanting centrifuge (28). 15. The apparatus of any one of items 10 to 10 14, characterized in that the device for dividing the digested sludge into a nutrient solution and the sludge concentrate is a gravitational sedimentation tank (17). Apparatus according to claim 15, characterized in that the gravity sedimentation tank (17) together with the device for dosing the coagulation agent is connected by a conduit (19), preferably comprising a pump (18), with a duplicator (20) and in the gravity sedimentation tank. (17) is provided: a mixing device, eg a paddle stirrer (17a). 17. The apparatus of any one of items 10 to 10 16, characterized in that the gravity sedimentation tank (17) is built between the heat exchanger (9) and the decanter centrifuge (28) and into the line (22) connecting the gravity: sedimentation tank (17) to the decanter: centrifuge (28) is built-in pump (23), on which: the suction line (22): a 'tube' (24) is connected, extending from: the upper part of the gravity sedimentation tank (17), and a 'line (25) is connected on its discharge side ) into a reservoir (26) to which is preferably connected: a conduit (27) for withdrawing the nutrient solution separated in the decanter centrifuge (28). 18. The apparatus of any one of items 10 to 10 17, characterized in that the reservoir (26) is arranged as a reservoir for the preparation of nutrient medium, which is preferably connected to a sedimentation reservoir (17) in a storage tank (40) with methanol as well as a source of bio-substances, (44), comprising a pump (43), connected to a fermenter (45). 19. The apparatus of any one of items 10 ' to 18, characterized in that a second storage tank (49) is built between the fermenter (45) and the separator (50). 20. The apparatus of any one of items 10 to 10 19, characterized in that it is provided with a powder dryer (58) configured to dry and stabilize the biomass. Apparatus according to claim 20, characterized in that a homogenizer (59) is arranged below the powder dryer (58) and below it is a weighing machine, preferably a bag weighing machine (60). Device according to one of Claims 10 to 21, characterized in that it has a device for drying and / or annealing the sludge concentrate, preferably a rotatable drying chamber (32). Apparatus according to Claim 22, characterized in that the rotary drying chamber (32) is connected to the decanter centrifuge (28) with the intermediate connection of the sludge concentrate container (29) and a homogenizer (33) is arranged below the rotary drying chamber (32) and below. weight, preferably bagging weight (34).