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WO2008098725A1 - Procédé et dispositif de traitement de boues d'épuration, d'eaux résiduaires ou d'une suspension de substances particulaires - Google Patents

Procédé et dispositif de traitement de boues d'épuration, d'eaux résiduaires ou d'une suspension de substances particulaires Download PDF

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Publication number
WO2008098725A1
WO2008098725A1 PCT/EP2008/001019 EP2008001019W WO2008098725A1 WO 2008098725 A1 WO2008098725 A1 WO 2008098725A1 EP 2008001019 W EP2008001019 W EP 2008001019W WO 2008098725 A1 WO2008098725 A1 WO 2008098725A1
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WO
WIPO (PCT)
Prior art keywords
suspension
sewage sludge
particulate substances
sludge
sewage
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
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PCT/EP2008/001019
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German (de)
English (en)
Inventor
Michael Richter
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Bionik Innovative Technik fuer die Umwelt GmbH
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Bionik Innovative Technik fuer die Umwelt GmbH
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Publication of WO2008098725A1 publication Critical patent/WO2008098725A1/fr
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Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/34—Treatment of water, waste water, or sewage with mechanical oscillations
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/06—Sludge reduction, e.g. by lysis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the present invention is in the field of wastewater treatment in industrial or municipal sewage treatment plants.
  • Biological wastewater treatment in industrial or municipal wastewater treatment plants usually involves the activated sludge process (also known as "activation process").
  • the wastewater is purified from organic contaminants by the metabolic activity of aerobic microorganisms contained in the biomass.
  • the biomass is a mixed biocoenosis of various types of microorganisms, the majority of which are flocculating bacteria and filamentous bacteria.
  • the activated sludge process the biomass is usually separated from the treated wastewater by sedimentation in a secondary settling tank or sedimentation tank, withdrawn from the bottom of the tank and partly fed as return sludge into the activated sludge tank and partly as excess sludge for digestion.
  • a sufficient ventilation of the waste water-activated sludge mixture with oxygen is required. This is usually done by aerators, with the help of compressed air or pure oxygen is introduced into the wastewater mixture.
  • the oxygen is needed for the oxidation of hydrocarbon compounds and ammonium.
  • the oxygen (O 2 ) is necessary in order to oxidize the ammonia (NH 4 ) which has a toxic effect on some bacteria via the intermediate nitrite (NO 2 ) to nitrate (NO 3 ).
  • This process is also called nitrification and requires the necessary bacteria (nitrifying agents) and a sufficient amount of dissolved oxygen.
  • COD chemical oxygen demand
  • the sludge age depends on the amount of sludge in the system and the daily sludge surplus due to the increase in biomass.
  • other processes such as denitifration (reduction of nitrate to molecular nitrogen) or the removal of phosphate in the activated sludge process, are discontinued.
  • the separation of the biomass in the secondary clarifier is an essential part. Due to the present in biomass Mischbiozönose of flocculating bacteria and filamentous microorganisms, the ratio of these types of bacteria in activated sludge for the sedimentation of biomass is of considerable importance.
  • One problem with wastewater treatment and treatment plants is the formation of undesirable bulking sludges and scum that results from increased growth of filamentous bacteria.
  • the filamentous bacteria have the property of aggregating into larger aggregates, thereby significantly hindering the above-described thickening and sedimentation process of the activated sludge. This has the consequence that a large biomass loss from the secondary sedimentation tank (so-called sludge output) occurs and the biomass content in the system decreases. As a result, the cleaning performance of the wastewater treatment plant or wastewater treatment plant can also be reduced.
  • scum formation In addition to the bulking sludge caused by filamentous microorganisms, scum formation also has a detrimental effect on the operation of sewage treatment plants or sewage treatment plants. Floating sludge is produced in particular by denitrification and development of bacteria with lipophilic surfaces.
  • Sewage sludge in sewage treatment plants is treated with ultrasound.
  • Ultrasonic treatment also destroys cellular structures of the microorganisms to a certain extent.
  • ultrasound sonotrodes are very expensive and consume a large amount electrical energy.
  • the digestion of the microorganisms and the homogeneity of the sludge decomposition is unsatisfactory.
  • WO 03/042109, US Pat. No. 6,200,486 and US Pat. No. 6,505,648 describe a method and a device for treating aqueous suspensions of organic substances or sewage sludge by utilizing cavitation forces.
  • Cavitation is the local formation and dissolution of bubbles or voids in liquids due to pressure fluctuations.
  • the cavitation bubbles are created by lowering the static pressure below the vapor pressure of the liquid, forming individual vapor or gas bubbles. According to the law of Bernoulli, the higher the velocity, the lower the pressure in a liquid. With increasing flow velocity of the liquid, there is a further pressure reduction. The gases dissolved in the liquid diffuse into the resulting bubbles or cavities. When the pressure in the liquid increases again, the vapor in the bubbles or cavities condenses and the gas bubbles collapse abruptly due to the external pressure. This results in very high local pressure and temperature peaks. Furthermore, the gas in the bladder is ionized and generates radicals that may be chemically reactive. Furthermore, the collapse of the bubble creates extreme local shock and pressure waves which result in a flow of fluid through the negative pressure of the collapsed bubble. These fluid streams are often referred to as "microjets" or "liquid jets”.
  • the suspension is conveyed under pressure through a nozzle having an initially narrowing and then widening cross-section.
  • the flow rate of the suspension is increased so much that the pressure of the liquid (typically water) falls below the vapor pressure, causing the formation of local gas-filled cavitation bubbles.
  • the subsequently widening cross-section of the nozzle it comes as a result of the sudden decrease in the
  • WO 2005/028375 has proposed a method and a device for comminuting particulate organic substances in suspensions of microorganisms, in which the formation of cavitation bubbles is avoided by the flow rate of the carrier medium (ie the (sewage sludge) suspension) is so high through a reaction space having a constriction that the carrier medium almost completely changes from its liquid phase to a homogeneous vapor phase.
  • the suspension to be treated is carried out through a nozzle which has a larger diameter in its inlet area and in its outlet area than the cross section in the central narrowing area.
  • the microorganisms or particle agglomerates contained in the suspension are subjected to a brief extreme acceleration and, if the vapor phase in the outlet region condenses back into the liquid phase, then exposed to an extreme delay.
  • Acceleration and deceleration forces will eventually produce the desired effects, e.g. Cell disruption and cavitation-free disintegration achieved while avoiding the locally occurring unwanted cavitation phenomena with the disadvantages described above.
  • the chemical oxygen demand is used to measure the biological activity of the digested sewage sludge in the activation process.
  • the COD value is a measure of the sum of all substances present in the water that can be oxidized under certain conditions. It therefore indicates the amount of oxygen that would be required for the oxidation of these substances, if oxygen would be used as a pure oxidant. Since a biological wastewater treatment plant with a proper function mainly dissolved, non-biodegradable organic substances in sewage sludge or wastewater are included and to a lesser extent biotically degradable organic matter and particulate organic matter, the COD value can be used to the streams of organic Describe carbon compounds in wastewater treatment plants. It is desirable to obtain the best possible reaction kinetics of the activated sludge process, for example, to assess the proportion of non-biodegradable organic substances, the oxygen demand in the activated sludge tank or the biological activity of the return sludge.
  • the process according to the invention for treating sewage sludge, wastewater or a suspension of particulate substances comprises:
  • step a) mechanical comminution of the coarse constituents contained in the sewage sludge, waste water or the suspension of particulate substances, b) homogenizing the sewage sludge, wastewater or the suspension of particulate substances treated in step a),
  • the device according to the invention for the treatment of sewage sludge, waste water or suspensions of particulate substances comprises:
  • Wastewater or the suspension of particulate substances contained coarse ingredients a disintegration device with a reaction space comprising a convergent channel portion and a constriction, wherein upon entry into the active space, a vapor stream is generated, which exerts a short-term extreme acceleration on the substances contained in the carrier medium and which condenses back into the liquid phase upon leaving the reaction space and thereby causes extreme deceleration forces, a contaminator with means for mixing or circulating the disintegrated sewage sludge originating from the disintegration device,
  • Waste water or the suspension of particulate substances are waste water or the suspension of particulate substances.
  • the device is suitable for preventing or reducing the formation of bulking sludge, floating sludge and / or foam in sewage sludge, waste water or a suspension of particulate substances.
  • the device can also be used to influence the Mischbiozönose in sewage sludge, wastewater or suspension of particulate substances, in which there is a decrease of filamentous microorganisms in favor of flocculating microorganisms in the sewage sludge, sewage or the suspension of particulate substances.
  • the process according to the invention for the treatment of sewage sludge, waste water or a suspension of particulate substances comprises a four-stage process in which, in a first step, a mechanical comminution of the coarse constituents contained in the sewage sludge, the wastewater or the suspension of particulate substances takes place. This is done in a crushing device in which a suitable cutting unit is arranged. After comminution in a second step, a homogenization of the comminuted mixture in a homogenizer.
  • the homogenizer is a circulation plant, with which a circulation of the sludge mass takes place.
  • the circulating system is a mixing axis extending transversely to the direction of flow and having mixing paddles mounted thereon.
  • the comminution and homogenization step ensures that no fluid-mechanical blockages occur in the subsequent disintegration step and all components of the sludge can be exposed to the disintegration step on an equal basis. Furthermore, an increase in the degree of disintegration can already be seen in the comminution and homogenization of the sewage sludge, which is reflected in an increase in the COD value (see FIG. 1).
  • the comminution and homogenization are part of a one-step process.
  • a thickening of the sewage sludge, wastewater or the suspension of particulate substances usually takes place.
  • a thickening TS of about 6% is particularly preferred.
  • the homogenized sewage sludge is fed to a disintegration device having a reaction space in which the liquid carrier medium of the sewage sludge, usually water, is subjected to a short-term extreme acceleration, whereby the vapor pressure of the carrier medium relative to the pressure in the Effective space is greatly lowered and the carrier medium is completely transferred from its liquid phase in the vapor phase.
  • a homogeneous vapor stream is generated, which briefly exerts an extreme acceleration when entering the reaction space on the sludge particles and releases extreme deceleration forces when leaving the reaction space when the vapor phase condenses back into the liquid phase.
  • a flow velocity must be achieved which is greater than the critical velocity for a phase change (liquid vapor) and which is characterized solely by the density of the water and the atmospheric pressure.
  • the flow velocity of Corresponds to critical speed, formed in the narrowest channel cross-section, a discontinuity surface over which the phase change of water into water vapor takes place.
  • the effective space essentially consists of a channel having a central constriction, which has a larger diameter in its inlet and outlet area than the central channel part with its constriction.
  • the reaction space comprises a convergent channel part with a narrowest channel cross-section.
  • the active space is a nozzle.
  • the diameter (d) and the length (I) of the nozzle are in a ratio of 1: 4 to 1: 6, preferably in a ratio of 1: 5 to each other.
  • the flow velocity in the inlet region of the reaction space is increased so much that the carrier medium of the treated suspension in the reaction space completely passes from the liquid phase to the vapor phase (i.e., to water vapor) and no cavitation bubbles are formed.
  • the steam flow is due to the increasing diameter in the
  • a flow velocity (u) of at least 28 m / s, preferably at least 42 m / s, preferably at least 50 m / s, is achieved in the reaction space (m / s meter per second).
  • Flow rate in a range of 42 m / s to 50 m / s is particularly preferred for the treatment of sewage sludge and has proven to be advantageous.
  • the transition to the vapor phase takes place at a critical speed u kr ⁇ t .
  • the critical velocity the formation of cavitation bubbles, which lead to the unwanted local effects, is largely avoided.
  • an influencing of the membrane surfaces of the microorganisms with release of surface-active substances (eg integral membrane proteins) and a dissolution of aggregates of filamentous bacteria takes place. Cellular breakdowns are also observed with the associated release of the cytoplasm and the biologically active substances dissolved therein
  • the disintegrated sewage sludge, wastewater or suspension of particulate matter (in short: the disintegrated mixture) are exposed in a fourth step to a reaction phase in a contaminant which allows the disintegrated mixture to act chemically and biologically.
  • a reaction phase in a contaminant which allows the disintegrated mixture to act chemically and biologically.
  • This will be the Mixture, optionally with agitation or stirring for a certain period of time collected in a reaction vessel and derived for further use. Both continuous operation and batch operation are possible.
  • the increase in the COD value already determined after the disintegration is again drastically increased (see FIG. 1).
  • the COD value is increased by at least 200%, in contrast to the three-stage process known from the prior art (without the fourth reaction step). Increases in the COD values of up to 400% or more can be achieved compared to the conventional three-stage process.
  • the COD increase in the four-stage process is in the range of 200% to 500%.
  • the disintegrated mixture from the disintegration step is preferably recirculated. This is achieved for example with a stirrer with vertical and / or horizontal stirring plates. By stirring the disintegrated sewage sludge additionally experiences an extreme increase in efficiency.
  • the process according to the invention mainly treat wastewater or sewage sludge (such as return sludge, excess sludge).
  • the method (as well as the apparatus described below) can also be used for other (aqueous) suspensions which contain particulate substances or particle agglomerates.
  • the suspensions may be a mixture in which microorganisms are contained and cell disruption is desired.
  • the device contains a pump whose power consumption is sufficiently high so that the high flow velocities of at least 28 m / s required for cavitation-free disintegration are achieved in the reaction space.
  • the invention further relates to a device or a plant for carrying out the method described above.
  • the device comprises
  • a crusher with means for crushing the coarse contained in the sewage sludge, sewage or the suspension of particulate substances
  • a homogenizer with means for homogenizing the sewage sludge, the waste water or the suspension of particulate substances
  • a disintegration device with a closed reaction space, in which the liquid carrier medium of sewage sludge, sewage or the suspension of particulate substances is exposed to a short-term extreme acceleration on entering the reaction space whereby the carrier medium is converted from its liquid phase into a homogeneous vapor phase, so that the substances contained in the carrier medium are subjected to a brief extreme acceleration, which subsequently passes through the effluent space upon exiting from the reaction space
  • Desintegrationsvortechnische derived disintegrated sewage sludge, sewage or the suspension of particulate substances Desintegrationsvortechnisch derived disintegrated sewage sludge, sewage or the suspension of particulate substances.
  • the crusher takes over the first, the homogenizer the second, the disintegration device the third and the contaminator the fourth process step of the method according to the invention.
  • the device or plant is a wastewater treatment plant.
  • the shredder is a conventional shredder, such as a rotary blade cutter, a knife mill, a shredder or a mill cutter, which breaks down the larger components into small components by attrition, grinding, shredding or cutting.
  • the homogenizer uses a mixer. Usually, it is a continuous mixer in which one or more mixing paddles are arranged on a mixing shaft in the flow channel. Such mixers typically operate at 1400 to 2800 revolutions per minute. However, other methods of homogenization are conceivable, such as the use of ultrasound, centrifugal forces or shear forces.
  • the device according to the invention contains means with which it is possible to bring non-disintegrated sewage sludge (or a suspension of particulate substances) into contact with disintegrated sewage sludge (or a suspension of particulate substances).
  • Such means include, for example, wiring systems, pumping systems or collection vessels.
  • For possibly repeated return of the sludge to the disintegration device means are provided, with which a return of the sewage sludge can be carried out in the disintegration device.
  • Such means include, for example, piping systems having the proper diameters and pumping circuits.
  • the effective space of the disintegration device consists of a constriction in which the diameter at the entry point of the active space and at the exit point of the active space is greater than the inner diameter at the constriction.
  • the reaction space is a nozzle.
  • the geometric conditions required for the effective space are preferably achieved when the diameter (d) and the length (I) of the nozzle are in a ratio of 1: 4 to 1: 6, preferably in a ratio of 1: 5 to each other.
  • the flow velocity u in the reaction space required for the vapor phase transition is at least about 28 m / s, preferably at least about 42 m / s and more preferably at least about 50 m / s, with speeds in the range from about 42 m / s to 50 m / s have turned out to be optimal.
  • the contaminator contains an agitator with vertical and / or horizontal agitator plates for circulating the disintegrated sludge mixture.
  • the additional reaction step in the method according to the invention can be a significant modification of some parameters that can be used to assess the performance and stability of a wastewater treatment plant, for example: increase in denitrification, increase in chemical oxygen demand (COD), increase in biochemical oxygen demand (BOD), decrease in power consumption (P tot ) / decrease in sludge volume index (ISV), decrease in oxygen concentration in the aeration tank.
  • COD chemical oxygen demand
  • BOD biochemical oxygen demand
  • P tot decrease in power consumption
  • ISV sludge volume index
  • 1 is a schematic representation of the four-stage process with crushing, homogenization, disintegration, contamination to achieve an intense biological activation with low power consumption
  • FIG. 1 shows the power expenditure (P x ) and the increase in biological activation (COD 1 ) in the individual phases (stages 1-4) of the method according to the invention.
  • the sludge to be disintegrated is first mechanically comminuted and homogenized in the homogenizer to form a homogeneous mass for the subsequent disintegration device. These two steps upstream of the disintegration ensure that no fluid-mechanical blockages occur during disintegration and that the constituents of the sewage sludge can be exposed to the disintegration process on an equal footing.
  • stage 1 mechanical disruption and the subsequent homogenization (stage 2) and the associated mechanical shear forces are already used to break up part of the microorganisms, resulting in a slight increase in the COD value (CSBi and COD 2 ). compared to the initial value (CSB 0 ) makes noticeable.
  • the following disintegration device is essentially a hydrodynamic one
  • the disintegrated sewage sludge originating from the disintegration device is subjected to a reaction time. This is preferably done by circulating the sewage sludge, so that the active ingredients such as enzymes and the living microorganisms contact each other and metabolic processes can proceed. In this, the disintegration downstream phase shows a drastic increase in the COD value of up to 500%.
  • the observed increase in the COD value depends on the biological activation achieved with the disintegration device, the size of the disintegrated mass flow and the residence time in the contaminant.
  • a significant COD increase can be detected in the contaminant, which clearly exceeds the COD increase by the disintegration device itself.
  • the COD value can be increased even further by passing the mixture through the disintegration device several times.
  • the bringing into contact of the sewage sludge is preferably carried out with a stirrer with low power consumption.
  • Process in particular by the disintegration downstream fourth reaction step, can be dramatically increased. Furthermore, the occurrence of swelling and floating sludge is avoided or reduced, and there is no need for external carbon sources (C donors) to stabilize the denitrification of the plant (data not shown).
  • C donors external carbon sources
  • the sewage sludge flowing through the convergent duct part (dA / dx ⁇ 0, duct cross-section A (x)) is put into a state which causes the water surrounding the microorganisms to evaporate.
  • a velocity u- ⁇ U k ⁇ t must be reached, which is characterized solely by the density of the water and the atmospheric pressure.
  • a usable effective space is only clamped at speeds u> u knt .
  • the length of the effective space l w > 0 can also be determined by the choice of the cross-sectional distribution A (x) of the divergent following the narrowest point
  • Channel part (dA / dx> 0) are affected and ends when the critical velocity u k ⁇ t is reached again in the divergent channel part.
  • the microorganisms leap abruptly into a flow field with speeds increased by a factor of 1000 as they enter the active reaction space, which then jump sharply as they leave the effective space by precisely this increase.
  • effects can be achieved ranging from the detachment of bioactive substances on the surface of the microorganisms to the disruption of the microorganisms and the release of the cell constituents by cell disruption.
  • the effects are essentially caused by the mass forces acting on the organic components of the sewage sludge when passing through the active active space.
  • Fig. 3 can be seen an existing vapor steam jet in the effective space of a disintegration device, which was made visible by means of a photographic image. Reaches the flow velocity u, the critical velocity u KNT and the evaporation pressure of the liquid is reached, a phase transition, whereby the particulate matter (especially microorganisms) present in the carrier media are subjected to a short-term extreme acceleration. At the end of the effective space increases its diameter, whereby the vapor stream is greatly delayed and condensed immediately. Due to these strong forces, the microorganisms and particle agglomerates are finally digested. Digestion by local cavitation effects (cavitation bubbles) would not lead to the observed result.
  • FIG. 4 shows a comparison of the COD increase with and without a subsequent reaction step (contamination). It can be clearly seen that with the additional reaction step, the increase in the chemical oxygen demand (COD value) can be significantly increased. Shown is the ratio CSB 4 to CSB 3 (ordinate) against time (abscissa). From one For a certain period of time, there is no further increase in the CS B value. As a result, the process according to the invention has an advantage over a process operated without this additional reaction step. Furthermore, the plants operated by utilizing the local cavitation and the disadvantages occurring there are avoided.
  • the anaerobic digestion (digestion) is reflected in a higher degree of digestion with shorter digestion times, a higher gas yield, a better stabilization result and an optimization of the sludge dewatering behavior.
  • aerobic degradation activation
  • stabilization of the biocenosis is observed.
  • the costs and the efficiency of the wastewater treatment process and the sludge treatment can be drastically reduced using the method according to the invention or the device according to the invention. This not only applies to the ongoing clarification processes, but also to all costs and material expenses incurred for the operation of the plant.
  • the device according to the invention is preferably designed as part of a sewage treatment plant for the cavitation-free disintegration of sewage sludge, also other applications of the combined disintegration below Use of the four-step process conceivable, such as the degradation of particle agglomerates or the digestion of microorganisms in aqueous suspensions.

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Treatment Of Sludge (AREA)

Abstract

L'invention concerne un procédé et un dispositif de traitement de boues d'épuration, d'eaux résiduaires et de suspensions de substances particulaires, ainsi que leur utilisation visant à éviter ou à réduire la formation de boues gonflées, de boues surnageantes et/ou de mousse dans les boues d'épuration, les eaux résiduaires ou une suspension de substances particulaires. Le dispositif selon l'invention comprend un homogénéisateur, un dispositif de désintégration et un contaminateur pour le traitement de boues d'épuration, d'eaux résiduaires ou de suspensions de substances particulaires.
PCT/EP2008/001019 2007-02-16 2008-02-11 Procédé et dispositif de traitement de boues d'épuration, d'eaux résiduaires ou d'une suspension de substances particulaires Ceased WO2008098725A1 (fr)

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DE102007007721.3 2007-02-16
DE102007007721A DE102007007721A1 (de) 2007-02-16 2007-02-16 Verfahren und Vorrichtung zur Behandlung von Klärschlamm, Abwasser oder einer Suspension partikulärer Substanzen

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WO2009047165A1 (fr) * 2007-10-05 2009-04-16 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Procédé et dispositif pour améliorer la désintégration de suspensions thixotropes grâce aux ultrasons
CN117125871A (zh) * 2023-08-23 2023-11-28 遂宁国润排水有限公司 一种污水处理厂浮泥资源化处置方法和处置系统

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DE102009059947A1 (de) * 2009-12-22 2011-06-30 BIONIK GmbH - Innovative Technik für die Umwelt, 65232 Verfahren zur Erhöhung der Gasausbeute in einer Gärvorrichtung, insbesondere einer Biogasanlage oder einem Fermenter, sowie Verwendung einer Vorrichtung zur Durchführung eines solchen Verfahrens

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