EP3541757A1

EP3541757A1 - Method for disinfecting and cleaning liquid media and method for separating solid and liquid constituents of a solid-liquid mixture and apparatus for implementing the method

Info

Publication number: EP3541757A1
Application number: EP17783388.6A
Authority: EP
Inventors: Alfons Schulze Isfort; Dominik Schulze Isfort; Frieda TAUBER; Otto Tauber
Original assignee: Individual
Current assignee: Individual
Priority date: 2016-11-16
Filing date: 2017-09-19
Publication date: 2019-09-25
Also published as: US20200055759A1; RU2019117891A

Abstract

The invention relates to a method for cleaning and/or disinfecting liquid and/or aqueous media, comprising the following method steps: cavitation treatment of the medium, in particular by means of jet cavitation, at a negative pressure < 1 bar, preferably 0.3 to 0.7 bar; subsequent treatment of the medium in a hydrodynamic reactor having a a rotating magnetic field and magnetic and/or magnetisable elements, in particular having ferromagnetic needles or a rotating cutting mechanism at a negative pressure < 1 bar, preferably 0.3 to 0.7 bar; subsequent separation, in particular sedimentation of the treated medium by means of sludge separation at a negative pressure of < 1 bar, preferably 0.3 to 0.7 bar. The invention further relates to an apparatus having the following features: a cavitator formed in particular as a jet cavitator, which is equipped with a negative pressure generator, a hydrodynamic reactor having a rotating magnetic field and magnetic and/or magnetisable elements, in particular having ferromagnetic needles and/or a rotating cutting mechanism, a unit for separation, in particular for sedimentation, preferably combined with a sludge separation apparatus.

Description

Method for sterilizing and purifying liquid media, and method for separating solid and liquid components of a solid-liquid mixture and apparatus for implementing the method

The invention relates to a process for the sterilization and purification of liquid and / or aqueous media and that initially to a method and apparatus for cleaning and especially sterilization of the medium and can for water treatment, in systems for drinking and household water, service water, in the chemical and pharmaceutical industries, in the food industry, in the medical industry as well as for the purification and sterilization of waste water from municipalities, industry, in agricultural enterprises, local sewage treatment plants, modular water treatment stations, but also in particular as a downstream process of previously for separating solid and liquid components of a solid-liquid mixture has taken place, for example, nachzubeteln liquid components, which have arisen in a process in which solid and liquid components of a solid-liquid mixture have been separated, for example in Behan tion of manure, ordnance and the like.

The current state of the art corresponds to numerous process technologies for multi-stage cleaning operations of liquid media such. B. water. The process techniques and systems used relate z. B. a chemical water sterilization such. As a water treatment with chlorine using special chlorine facilities, where the treated chlorine water is then mixed with the whole incoming water mass. One disadvantage of chlorine water treatment is that chlorine must be stored in intermediate storage tanks for use in steel cylinders, which results in high investment costs. Water treatment plants can not prevent the penetration of significant amounts of inorganic and organic substances into drinking water. Under these conditions, the use of chlorine as a degerming agent leads to the formation of new compounds, which are often more toxic than the starting materials. It is well known that water treatment with chlorine produces compounds containing halogens, most of which are mutagenic and some of which are carcinogenic to human health. The chlorination of phenol-containing water enhances z. B. the water odor due to the formation of chlorophenols, the threshold concentration is a thousand times higher than that of the actual phenol.

The most common strong oxidizing and disinfecting agents are molecular chlorine and its modifications, hypochlorides, chlorammonium (B. Sostmann "Organoleptic Testing of Water", M .: Chemie, 1984).

It is a method for the treatment of water and water solutions is known, which provides a pH correction by a multi-stage pressure reduction in a high-pressure liquid, with their return reaches the value at which the cavitation begins with subsequent increase in pressure to the value at which the cavitation ends. Subsequently, the circulating liquid is preheated, then removed a portion of the high pressure liquid for filtration and withdrawn the cavitated liquid under pressure from the remaining circulation flow, cooled and turned off until cavitation bubbles implode and the resulting solids are deposited. Thereafter, the stabilized liquid is returned to the low pressure circulating flow. The pressure of the cavitating liquid is brought up to air pressure values or higher. The energy gained from cooling the flow is used as a heat transfer medium for household and process requirements. The cavitation is performed by hydrodynamic or ultrasonic methods. The implosion of bubbles occurs during cooling of the cavitated liquid by feed and / or cold flow of the heat carrier. With the stream of the liquid taken for filtration, the filtered solids are rinsed (Patent RU 2240984 dated 27.11.2004).

The drawbacks of this technical solution include a low disinfecting efficiency, which is required for the drinking water. Furthermore, it is impossible to remove organic matter. The implementation of the method, as disclosed therein, therefore seems doubtful whether this is to be realized at all.

There is also known a method of extracting water from natural resources, wherein the water from an open water is first cleaned in a prefilter and then ultrafiltered in a coarse filter. The aftertreatment, until the water has the quality of drinking water, is done by reverse osmosis. To For sorption on coal, drinking water is consistently subjected to cation and anion exchange. Thereafter, the water is sterilized in a cartridge filter with pore size of 0.2 μηι. The water quality is continuously tested according to the values of a specific electrical resistance (Patent RU 2258045 dated 10.08.2005).

The plant for implementing the common method consists of a coarse filter, a pre-filter, a pump, a supply line, an ultrafilter, a high-pressure pump, a reverse osmosis filter, resistance meters, a carbon filter, a Soptionsfilter, a cation filter, an ion filter and a candle filter for sterilization.

A disadvantage of this method and the apparatus for carrying it out is that there is no pre-oxidation to convert soluble iron to hydroxide to prevent its penetration into the microfilters. Iron ions in the microfilter, their frequent regeneration or exchange interfere with the continuous operation of the membrane plant, increase maintenance costs and cost of drinking water production. Carbon filters, sorption filters and candle filters collect pollutants. They must be flushed regularly with chemical reagents.

The prior art discloses a device for sterilizing sewage and natural waters (Patent RU 2328450 of 10.07.2008), which consists of five stages, each of which has a container and a hydrodynamic cavitator. Each hydrodynamic cavitator is in the form of a rotating cavitator with a Suction and a discharge nozzle executed. The container of the first stage is connected to the suction port of the cavitator, the discharge nozzle is connected to the container of the second stage. The second stage cavitator is connected to the nozzles with second and third stage containers. The third-stage cavitator is connected to the sockets of third and fourth stage tanks. The fourth stage cavitator is connected to the sockets of fourth and fifth stage tanks. The fifth stage cavitator is connected to fifth stage vessels and the water clarification device. Bottoms of the fourth and fifth stage tanks are connected by piping to the sediment draining device.

A disadvantage of this method is that similar functional components are used, namely rotating cavitators, which can not provide some necessary factors of neutralization and cleaning operations such as mechanical impact processing, electrolysis processes and so on.

The prior art further discloses a process for purifying liquid media, which includes balancing the medium composition, cavitation treatment of the medium, treatment of the medium in the magnetic field, pH correction of the medium, and sedimentation to clarify the medium (Patent application RU 2002119765). Furthermore, a method and a device for the treatment of liquid media by jet cavitation are known in the prior art (RU Utility Model Patent 54662 of 10.07.2006).

Furthermore, a method for treatment by means of a rotating pulse device is known (Patent RU 2304561 dated 20.08.2007).

The disadvantage of the above-mentioned method and treatment plants is that they can not ensure high cleaning performance and high efficiency.

In the context of the present invention, said technical result is achieved by variants of the procedure as follows:

- The treatment with Strahlkavitation and in the ferromagnetic stator is carried out to form strong oxidizing agents ΟΗ +, H2O2 and O3, each at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar;

- Optional treatment in the ferromagnetic stator with dispersing of particles down to submicron dimensions and enlargement of the phase interface gas-liquid-solid and again at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar;

- Before the cavitation treatment, an optional adjustment of the aqueous medium takes place; - During the hydrodynamic treatment, at least one reagent is optionally added to the ferromagnetic stator. The reagent may, for. Example, be selected from the following group: milk of lime, aluminum sulfate, iron chloride and this is carried out at a reduced pressure of <1 bar, preferably 0.3 to 0.7 bar;

The method may involve treatment of the recovered medium in a rotating pulse device and again at a negative pressure of

<1 bar, preferably 0.3 to 0.7 bar;

- The method may optionally include filtering the medium by means of a Tiefbettfilters and again at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar;

The method may optionally include ozonization of the medium at

<1 bar, preferably 0.3 to 0.7 bar;

The method may optionally comprise a treatment of the medium with UV rays at a reduced pressure of <1 bar, preferably 0.3 to 0.7 bar;

The method may comprise a sedimentation aftertreatment in a z. B. multi-stage cascade of sedimentation and again at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar.

The above technical result is achieved by implementing the method described for the purification and sterilization of aqueous media, in particular, that in the implementation of the method, the following device units are used: a cavitator, in particular a Strahlkavitator, at a negative pressure of <1 bar, preferably 0, 3 to 0.7 bar, with a ferromagnetic stator with a magnetic rotating field and a magnetic and / or magnetizable element, in particular with magnetic and ferromagnetic needles or a rotating cutting mechanism, and preferably with a unit for sedimentation, in particular a separation device and in particular a downstream sludge separation system, which also at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar is operated.

Furthermore, said technical result in individual implementation variants of the device is achieved in that the device can optionally be equipped with a compensating mixer, which is installed in the flow direction of the media to be sterilized in front of the Strahlkavitator. Furthermore, the device may optionally be equipped with a means for metering reagents for the ferromagnetic stator. In addition, the separating device of the medium may preferably be equipped as a hydrocyclone. Furthermore, the device or the system can be equipped with a rotating impulse device, which is installed in the flow direction of the media after the separation device. The device is preferably equipped with deep bed filters, which are installed downstream of the separation device. Furthermore, the device may preferably be equipped in a unit for ozonization of the medium, which is installed in the flow direction downstream of the separation device. Furthermore, the device is preferably equipped with a unit for UV irradiation of the medium, which in the flow direction the separator is installed. In addition, an automatic control unit can be provided to automatically set and control the entire device and thus the process line.

In contrast to known analog systems, the method according to the invention and the system suitable for implementing the method use a combination of a cavitator, in particular a Strahlkavitators with a system which is equipped with a negative pressure and a subsequent ferromagnetic stator (FMS) with magnetic rotating field and magnetic and / or magnetizable elements, in particular with ferromagnetic needles.

It was unexpectedly found that the cavitation treatment at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar in the cavitator and subsequent cavitation treatment of the medium in a ferromagnetic stator (FMS) in a mechanical cutter performance and efficiency the cleaning significantly increased. This is due in particular to the following:

In a conventional treatment of waste water with a Strahlkavitator a Kavitationsbereich L is formed. Within this cavitation area L run the degradation of molecules, the formation of radicals and the bubble implosion. After passing through this cavitation region L, the liquid flow starts to stabilize, which means that the reaction of ozonolys, the degradation of water and others begin to run backwards and reach a balanced value. The lifetime of the strongest oxidant OH radical is approximately 100NS. That means, that after passing through this region L no radical OH occurs in chemical reactions more. Accordingly, the processes for the treatment of the liquid in the Strahlkavitator and in the FMS are split in time and represent independent individual operations.

The negative negative pressure results in larger cavities, in particular supercaverns, a cavitation area which is characterized by a hundred times the length L1 (with the same conductor cross-sections). In the end, the cavitation number drops, in particular, to a stable supercavitation operation. These cavities, and in particular a supercaverne, produce water loss products, radicals, cavitation nuclei and form them directly in the working area of the FMS for reduction-oxidation reactions, displacement reactions and other reactions that take place on huge phase interfaces EFF (gas-liquid-solid), which are within the working range of the FMS arise. Consequently, concurrent cavitation processes, the formation of strong oxidants, interactions between oxidants and degraded liquid compounds on multiply increased phase boundaries occur in the working area of the FMS, which increases the reaction rate by a multiple and by comminution of solids down to the submicron range and the enlargement of phase interfaces ensures a complete interaction between all the elements involved in the reaction. Accordingly, the general efficiency of displacement, sedimentation, oxidation and other processes increases, which significantly improves the cleaning quality. The speed of the subsequent separation, in particular a sludge sedimentation is ensured. In the ferromagnetic stator in addition reagents, eg. As lime, be used for acceleration of reactions. Furthermore, after the separation device, the medium can be subjected to a post-purification and after sterilization by means of a rotating pulse device, a deep bed filter, an ozonization unit and / or a UV treatment unit.

A conventional plant or apparatus for implementing the described method comprises sequentially a balancing mixer, a continuous jet cavitator a vacuum generator a ferromagnetic stator with rotating ferromagnetic elements (magnetic rotating field), combined with a metering unit for the addition of reagents, a unit for sedimenting equipped z. B. with hydrocyclones and a sludge deposition system, a rotating pulse device (cavitator), a Tiefbettfiltereinheit with automatic filling Regeneration, an ozonization unit, a UV irradiation unit and a unit for supplying treated water. Furthermore, an automatic control unit can be provided, which is linked to all facilities of the system. Other facilities are installed if necessary to fine clean, z. B. to win drinking water.

The balancing knife is intended for balancing the composition of the liquid medium and represents a container with a mixer. The Strahlkavita- tor is intended for the treatment of the liquid medium. A beam cavitator generally consists of a tube housing with a narrowed and a rear extended part, as well as with a nozzle for applying the negative pressure. A ferromagnetic stator (FMS) is designed for the cavitation treatment of the medium to accelerate the oxidation and degradation of molecules of organic matter dissolved in water. The FMS uses the energy of the rotating magnetic field with a high specific concentration in a room of the working area. The FMS includes a housing with a working area containing a replaceable insert and ferromagnetic elements (needles) and an inductor that extends over the entire working area. The inlet of the FMS is directly connected to the outlet of the cavitator. The sedimentation unit equipped with a sludge separator is intended for the separation of the liquid medium and the sludge resulting from subsequent treatment.

A rotating pulse device is designed for the subsequent removal of suspended matter from the cleaned medium. It is a horizontal cylindrical hollow housing having two diametrically opposed threaded bores in which the nozzles are arranged, the mouth of which is made flush with the cylindrical inner cavity. The cylindrical hollow housing also has a cylindrical hollow rotor coaxial with the gap. The cylindrical hollow rotor has two diametrically opposed identical openings. In this case, identical orifices of the nozzles and two identical openings of the rotor lie on a diametrical axis. The rotor is equipped with a bearing unit equipped, which is equipped with a collar for sealing the housing interior of the hydrodynamic pulse generator upon rotation of the rotor of an electric drive. Tiefbettfiltereinheiten, ozonation units and the UV irradiation unit provide a final fine cleaning of the corresponding medium.

In the following, the implementation of the method according to the invention by means of the above-described system using the example of a wastewater treatment will be described.

A waste water is introduced via equalizing mixtures at a rate of 28 to 33 m / s in the Durchlaufkavitator, where the Kavitationsbehandlung of wastewater takes place. In this case, a negative pressure of <1 bar, preferably 0.3 to 0.7 bar is applied in the flow-through cavitator. This creates a supercaverne and their main footprint is increased. Thus, the cavitation process is in the phase of Ventilation cavitation (artificial cavitation), which is characterized by a reduction in the Kavitationszahl (stable supercavitation operation). In an implosion of microbubbles, cumulative microbeams occur at velocities of 200 to 1,000 m / s and a local impact pressure of about 10 ³ MPa, which act on reaction components at intervals comparable to molecular dimensions. Furthermore, in a collision of impulse jets, Pils and bacteria spores are killed at lightning speed.

A prerequisite for a bubble implosion is the movement and excitation of the medium, resulting in a spherically symmetric bubble implosion Has. A very high speed at the time of implosion and a strong increase of local pressure are considered as one of the causes of the formation of cavitation. It is known that cavitation is a phenomenon of vapor formation and of air excretion caused by pressure reduction in the liquid. The cause of cavitation is the sieving of a liquid at normal temperature under low pressure. The emergence of cavitation allows the air dissolved in the water, which excretes when pressure decreases. The life cycle of a cavitation bubble consists of two phases: expansion and implosion, which together form a complete thermodynamic cycle. When ready for printing, the hydrostatic pressure decreases, so that the forces acting on the liquid molecules are greater than the molecular binding forces. Because of the rapid change in the hydrostatic equilibrium, the liquid explodes, producing several micro bubbles. The cavitation occurs earlier, the more "dirty" the liquid is with solids or other foreign bodies (eg bacteria), the higher their temperature is.

The "boiling" of a liquid is due to the fact that a thin layer of air is adsorbed on the surfaces of these particles. The air-layer particles, when they enter the vacuum area, allow the development of such cavitation.

The bacterial flora in the liquid to be treated also serves as a place of origin for cavitation bubbles. When the liquid is ready in the vacuum When it reaches boiling point, cell membranes of bacteria that reach the center or near cavitation bubbles are completely or partially destroyed because of the pressure difference inside and in the environment.

The second phase of the life cycle of a cavitation bubble is the implosion (condensation). This takes place in a pressure range into which the cavitation bubble with the liquid to be treated passes. The condensation process of a cavitation bubble takes place instantaneously. The liquid particles surrounding the bubble migrate at high speed to their center.

Ultimately, the momentum of particles at the moment of bubble formation triggers local hydraulic micro-shocks accompanied by local pressure increase up to 10 ⁴ kg / cm ² and local temperature increase to 1000-1500 ° C. In the course of hydrodynamic cavitation at high speeds of the working media in the cavitators of 28 to 33 m / s most cavitation bubbles are deformed and are elliptical or conical. The implosion of such bubbles creates cumulative, high-energy rays that destroy everything in their path. The implosion of individual cavitation bubbles shows no expected effect. However, there are several cavitation bubbles present and several thousand implode per second. Therefore, they can collectively exert a significant destructive or other effect without heating the liquid to be treated. Consequently, cavitation in ultra-high temperature operation, in addition to the mechanical influence, also has a microsterilizing effect on the bacterial flora in the zone of extinction of cavitation bubbles. The Walls of cavitation bubbles and liquid drops that are in bubbles have unlike charges. In an implosion, the bubbles shrink drastically and the charges come on very small surfaces of the bubbles. By a jerky reduction of surfaces of cavitation bubbles, the voltage of static electricity increases dramatically. Between the walls of cavitation bubbles and drops that are inside, there are electrical discharges that have a form of microscopic lightning. These high intensity electrical discharges also have a detrimental effect on the bacteria causing the bubbles to form.

High temperature and high pressure generated in the zones of extinction of cavitation bubbles as well as micro flashes of static electricity cause the water decomposition process.

Accumulation of cavitation on surfaces of bacteria surrounded by adsorbed air is accompanied by the formation of free radicals OH, HO2, N as well as N products of their recombination H2O2, HNO2, HNO3. The formation of hydroperoxide, free radicals and acids has a lethal effect on the bacterial flora of the fluid to be treated.

With a liquid flow, the gas-air phase, which contains a large amount of gas and non-imploded bubbles as well as nucleons (cavitation nuclei), is transferred to the working area of the FMS. In the working area of the FMS is a Shredding of solids contained in wastewater to sub- micron dimensions as well as a molecular degradation under impact of ferromagnetic elements in the magnetic rotating field. There are further cavitation effects and electrolysis processes take place.

Under the action of the electromagnetic field, the ferromagnetic elements rotate about their transverse axis in the working area of the FMS at a speed close to the speed of rotation of the magnetic field to migrate simultaneously within the working area. In addition, the particles oscillate with respect to the force vector of the magnetic field. These vibrations can be several thousands per second. As a result, each ferromagnetic element constitutes its own mixer mill which rotates at a high but varying rotational speed. Such movement of hundreds of particles results in rapid stirring and dispersion of components. The specific energy of the rotating electromagnetic field is extremely high and reaches 10 kW / m ³ . The energy intensity of the FMS is z. B. 100 to 200 times higher compared to the energy intensity of vibration mills.

In this way, a highly dispersed heterogeneous system GFF (gas-liquid-solid) is formed in the working area of the FMS, which occurs at a high rate in reaction with radical OH, H2O2, O3 and even with atomic oxygen. Acceleration from the rate of chemical reaction is due to multiple enlargement of contact surfaces of the phases at the boundaries to the GFF. To accelerate the precipitation of solids (heavy metals) and for the additional disinfection of waste water, reagents are added to the FMS by means of a dosing system, eg lime milk, aluminum sulfate, iron chloride (depending on the original composition of the wastewater).

Since the reagents are introduced directly into the working area of the FMS and are comminuted together with solids from waste water, they immediately enter the precipitation reaction and the displacement reaction with heavy metals. Transfer processes from hexavalent chromium to trivalent chromium and then to chromium hydroxides (heavy metals Zn, Fe, Cu), which are located in the wastewater in the working area of the FMS, are converted into the insoluble hydroxides Fe (OH) 3, ZN (OH ) 2 and Cu (OH) 2. Organic substances are broken down to complete mineralization (up to CO2 and H2O). The treated effluents are introduced into the unit with hydrocyclones, where accelerated sedimentation of coagulated particles occurs. Mud is removed with the purging system.

If needed for fine cleaning, the purified water passes through the rotary impulse device (cavitator) or through a floatation floatation unit through the deep bed filter unit, ozonation unit and UV irradiation unit to sanitize the water according to the end user's requirements for the treated water. All devices and units are controlled by an automatic control unit. Examples of the implementation of the method according to the invention are described below.

Example No. 1:

The purification of waste water from a slaughterhouse was carried out on a plant with a capacity of 5 m ³ / hour according to the methods described above. Table 1 shows results of a quantitative chemical analysis (QCA) of the water before and after treatment and the purification efficiency in terms of permissible limit values (BGW values).

32 strontium, mg / dm ³ 1, 46 0.38 74

Example No. 2:

The neutralization of wastewater from pigsties was carried out on a process line with a capacity of 5 m ³ / hour according to the method described above. Table 2 shows water levels before and after treatment.

Value before treatment after treatment

Total number of microbes, m. t / ml. 4 10 ⁷ Without findings

Worm egg content, St / dm ³ 3 10 ⁴ Without findings As a result, the process and process line illustrated by intensifying processes that occur in the caviator, FMS, and cutter greatly increase the cleaning performance, as well as the efficiency of cleaning and sterilizing liquid media.

Although the method in question and the process line are described by way of example of wastewater treatment, they can also be used for the sterilization and purification of other liquid media. For example, the process described above may be followed by a process in which solids and liquids are separated from a solid-liquid mixture to after-treat the separated liquid

The solid-liquid mixture is separated in the upstream process in a housing with a vibrating screen. In this case, prevails in the housing such a negative pressure above the vibrating screen and below the vibrating screen, so that with the set pressure reference with a pressure gradient in the direction of the space below the vibrating screen of the solid-liquid mixture with the set vibrations during the separation process in a kind of limbo above the screen surface can be held, so that this state can be stabled by the pulses from the vibrating conveyor with conveying direction in the direction of the slightly rising vibrating screen. Due to the prevailing pressure conditions, the material to be separated is flowed through by air entraining liquid particles. Below the suspended cake to be separated (solid-liquid mixture), an air flow can also pass through the meshes of the sieve surface with entrainment of corresponding liquid fractions, so that the separation process takes place at an exceptionally high process speed and the vibrating sieve is permanently cleaned.

It is useful if in the course of further promotion of the solid-liquid mixture results in a breaking edge within the screen surface, so that this is divided into at least two Schwingsiebbereiche, in such a way that results in the stepped training in the conveying direction a lower Schwingsiebfläche with the result that the further conveyed liquid-solid materials can be turned by an overhead movement and the previously promoted upper side of the cake to be separated on the previously upper side comes with a corresponding pulse, whereby the Separierungsvorgang is further promoted.

By a pressure equalization between the space below the vibrating screen and the space above the vibrating screen, which takes place automatically and, for example via a flexible seal, such as a flexible rubber lip, can be adjusted, it is also ensured that no setting of the material to be separated on the upper screen surface takes place, since in this case an automatic pressure equalization takes place with an initial setting. This is extraordinary achieve high performance data with the method according to the invention and with the device according to the invention.

Because of such excellent performance data, the method and apparatus of the invention have been found to be particularly suitable for a variety of different applications, such as the chemical industry

including the petrochemical industry

Ores, minerals

Alumina industry

Coal industry

Energy Industry

Engineering / Plant

• food industry, eg. B. for the processing of slaughterhouse waste

• Beverage industry

health service

disaster Relief

Pharmaceutical industry

Agriculture, e.g. for processing manure or for municipal applications, eg. B. Treatment of sewage sludge

Power generation of peat Production of organic fertilizer

Conversion of biomass into coal products • general biomass processing

Advantageously, it can be provided that the inlet, through which the solid-liquid mixture reaches the vibrating screen, opens above the rear end of the vibrating screen in the conveying direction. The solid components in the solid-liquid mixture reach the vibrating screen in the region of its rear end so that they are conveyed over the entire length of the vibrating screen until they reach the front end where the discharge opening is provided. The movement of the solid components along the length of the vibrating screen promotes the separation of the liquid constituents from the solid constituents and thus increases the degree of separation.

Advantageously, a distributor can be arranged in the housing below the inlet and above the vibrating screen. This distributor is used to optimally exploit the surface of the vibrating screen for separation. The distributor does not act in the longitudinal direction or conveying direction of the vibrating screen, but transversely thereto, so distributes the mixture over the width of the vibrating screen and advantageously over its entire width.

Advantageously, the vibrating screen can be arranged obliquely from bottom to top and operated so that it promotes the solid components obliquely upward. The inclination of the inclination can be specified constructively in adaptation to the intended application or it can be a tilt adjustment be provided of the vibrating screen or the housing to flexibly adapt the device to different requirements can.

It can be particularly advantageously provided within the housing in which the vibrating screen is to adjust the level of the solid-liquid mixture only so high that the vibrating screen protrudes partially above this level upwards. Already within the Fes liquid mixture applied to the vibrating screen, a kind of floating filter cake with a high solids content forms on the vibrating screen. This filter cake is promoted on the vibrating screen upwards and thus beyond the level of the solid-liquid mixture, so that there, supported by the vibrating effect of the vibrating screen, a particularly effective further separation of the liquid components from the filter cake can be done before the solid Components then enter the discharge opening, through which they leave the housing.

In practical experiments, a mesh size of the vibrating screen has proven to be smaller than 0.8 gm, for example, between 0.7 and 0.8 pm. When separating manure, high throughput rates of the device were achieved with such mesh sizes. While the proportion of solid constituents within the solid-liquid mixture was about 7 to 8%, it was only about 0.8% in the liquid components coming out of the device. With the help of an even smaller mesh size of for example about 0.4 to 0.5 pm, the degree of separation can be increased even further and, with the same starting material, the amount of solid constituents can be reduced to about 0.2 to 0.3%, at the expense of one lower throughput of the device.

The degree of separation can be further improved if the solid constituents coming from the discharge opening are aftertreated in a subsequent second separation step, for example in a screw press. A particularly advantageous embodiment of a screw press is that this has in known manner a screw, which is referred to as press screw or screw conveyor, and has one or more filters radially outside the screw. This post-treatment can also be carried out under reduced pressure, as m claim 1 advantageous and carried out according to claims 2 and 3. The particularly advantageous embodiment is that this filter has a plurality of slots extending in the longitudinal direction of the screw. Liquid components emerging from the material need therefore not flow transversely to the conveying direction of the screw radially outwards in the manner of a change in direction of about 90 °, but they can due to the longitudinal slots extending with little change in direction over the entire length of the screw and continue to pass radially outward and through the slots. As a result, not only the operation of the screw press with a surprisingly low drive power is possible, but it also excellent results are achieved, which relates to the increase of the dry content in the material. The configuration of the screw press described can be advantageous comprise a filter having a plurality of flat iron. These flat bars are aligned coaxially with the worm by the flat iron extending lengthwise in the longitudinal direction of the worm. As far as the material cross-section of the flat irons are concerned, they are aligned around the worm radially, so that the width of the flat iron extends radially outward from the worm and the thickness of the flat iron extends in each case tangentially to the worm. Because of this radiate ring-like orientation of the flat iron these lie with their radially inner ends almost close to each other, while outwardly the distances of the flat iron are larger to each other. Even if the individual flat iron seem to rest against one another gap-free and form a tube apparently tightly surrounding pipe, where only visible on its radially outer surface columns, the pressing pressure of the screw is sufficient to moisture that is still present in the material through to drive the minimum gaps between the flat irons and thus to improve the degree of separation and to further reduce the moisture content in the solid components.

In comparison, for example, to provide a pipe wall with a variety of fine slots, a structurally simple and economically producible design of this filter, for example, consist in that each several flat iron are combined into a package, for example, depending on the thickness of two to ten adjacent flat iron. Despite the fact that the individual flat irons abut one another over the entire surface, a sufficiently high level of nendruck within the filter Durchtrittsmöglichkeiten for the liquid to be discharged. Spacers are provided between two adjacent packets in the outer radial region of the filter, but not in the radially inner region of the filter so as to give an overall annular and nearly circular cross-section of the filter surrounding the press screw in the manner of a polygonal tube. Also independently of the proposed device, which has a suctioned vibrating screen, the screw press can be used for separation.

Advantageously, a conveying device can be provided which conveys the solid components which either arrive directly from the housing accommodating the vibrating screen or indirectly, namely from the downstream second separation stage, to a transfer point. The conveyor can be configured in many ways, for example as a conveyor belt or screw conveyor, wherein a screw conveyor is mentioned below purely by way of example. At this transfer point, the solid components are transferred from the device to a subsequent device. The downstream device may be, for example, an open storage bin or a container into which the solid ingredients are added. The solid constituents, if they lie as a pile on a substrate or are filled in a container, even after days a considerable temperature level, possibly due to Kompostierungsvorg- gene. The solid ingredients can therefore be given for example in a container, the one Includes piping heat exchanger, so that a guided through this heat exchanger medium is heated. Advantageously, the proposed device can be designed as a mobile, transportable unit, z. B. be constructed within a container, on a vehicle trailer or the like. In practical experiments, it has surprisingly been found that due to the high throughput capacity of the contents of a complete manure tank, as can be found on farms, can be separated within a few hours. For this purpose, a supply line from the manure tank is moved to the device, through which the manure from the manure tank enters the device, namely in the housing, which surrounds the vibrating screen. In this feed line, a pump is advantageously provided, which promotes the solid-liquid mixture into the housing.

The aforementioned suction pump in turn promotes the liquid components in the manure tank back and ensures the negative pressure below the vibrating screen. By this circulation, it is not necessary to provide an additional tank as an intermediate storage, in which the coming out of the device, separated, liquid components of the manure are directed. Rather, the proportion of solid components in the manure container is gradually considerably reduced by the circulation of the manure or its liquid components, so that after a few hours of treatment, for example, three to five hours, the liquid in the slurry tank a solids content of only about 1 % or even less. Because of this short treatment time, a particularly economical use of the proposed device may be that it does not remain permanently unused for a long time next to the slurry tank, but rather is spent from day to day to another slurry tank, for example by a contractor. The embodiment of the device as a movable trailer or the arrangement of the individual components of the device on a mobile trailer allows this mobile use of the device.

If the device is stationary, the solid-liquid mixtures in containers, by tank truck or the like can be spent on the device. For example, by means of a stationarily operated device, the solids content can be separated as completely as possible from the solid-liquid mixture and can be thermally utilized in a combustion plant which is also stationary there. A stationary device is not subject to the limitations imposed on a mobile device, for example, in terms of its dimensions, so that stationary devices can be made particularly efficient.

Apart from the regularly mentioned field of application of liquid manure separation, the device can be used in the agricultural sector, for example for fermenter cleaning by the contents of a biogas fermenter is freed, for example, of mineral solids such as sand. This will prevent the fermenter from slowly becoming silted up and its entire useful volume will be through made such cleaning available again. The essential for the function of the fermenter microorganisms are advantageously recycled to the fermenter by the liquid components are recirculated from the device in the circulation in the fermenter.

Advantageously, it can be provided that the device is equipped not only with a single vibrating screen, but with two vibrating screens. These two vibrating screens are each arranged in a separate housing. In this context, it is provided that the solid-liquid mixture is led to both housings separately by branching a feed line, which brings the solid-liquid mixture to the vibrating screens, and a separate inlet is provided in each of the two housings. By using two vibrating screens, the performance of the device is substantially doubled, without having to create a single vibrating screen with correspondingly larger, for example, doubled dimensions, which involves considerable design challenges. By comparison with such a large vibrating screen smaller vibrating screens can also cascade the performance of the device in finer stages and adapt to different needs by accordingly two, three or more vibrating screens are operated. In particular, in the case of stationary devices, this can be provided without problems, since here the road admission-dependent maximum dimensions do not have to be considered. The arrangement of two housings and two vibrating screens can also be advantageously used to achieve a particularly high degree of separation, in that the two vibrating screens have different mesh sizes:

By means of a valve arrangement, a switch can be made possible to selectively lead the solid-liquid mixture to only one of the two inlets and thus to only one of the two different vibrating screens. Thus, for example, the solid-liquid mixture can first be led out of the manure tank into the housing, in which the vibrating screen with the larger mesh size is located. Later, the valve assembly can be switched so that the solid-liquid mixture, which now already has a significantly lower solids content, is placed on the vibrating screen with the smaller mesh size, so that now even more, previously unfiltered solids by means of this vibrating screen from the solid Liquid mixture can be separated. The separation of initially coarser solid constituents by means of the first, coarser-meshed vibrating screen prevents the fine-meshed vibrating screen from becoming too covered and too impermeable by the solid constituents, which would adversely affect the throughput.

In addition, the two differently configured vibrating screens with their different mesh sizes can be used to select in adaptation to the particular starting material present, for example, differently composed Güllesorten, each of the most suitable vibrating screen. This can be used in particular for the already mentioned wage companies or mobile ones Be advantageous devices that are spent at different locations and are therefore charged with possibly very different starting materials.

As an alternative to the mentioned switching of the valve arrangement, the vibrating screens of different mesh sizes can be connected in series so that the liquid constituents are led out of the coarser vibrating screen onto the finer vibrating screen and only then out of the device.

However, the valve assembly can also be designed so that it allows four different modes: either the solid-liquid mixture is performed only on one of the two vibrating screens, namely either first on the one or secondly the other vibrating screen, or third is the hard Liquid mixture in the manner of a parallel operation led to both vibrating screens, or fourth, the solid-liquid mixture is performed in the manner of a series or series operation on only one and then the other of the two vibrating screens. The corresponding configuration of the valve arrangement and associated piping guidance is known to the person skilled in the art, for example by means of shut-off valves or reversing valves, in particular multiway valves, and therefore does not need to be explained in detail in the context of the present proposal.

The solid components that form a filter cake resting on the vibrating screen cause a certain sealing of the vibrating screen. This seal is advantageous insofar as it prevents or reduces the suction of air that could otherwise be sucked in by the vibrating screen where an obliquely upward vibrating screen protrudes upwards out of the solid-liquid mixture. This sealing by the filter cake therefore enhances the suction power in the area where the vibrating screen dips into the solid-liquid mixture and where the liquid from the solid-liquid mixture is to be sucked down through the vibrating screen.

Advantageously, an overflow edge can therefore be provided on the forward end of the vibrating screen in the conveying direction, which extends upwards beyond the vibrating screen. It has the effect that a certain minimum layer thickness of the mentioned filter cake has to be reached and maintained on the vibrating screen before the solid components can overcome this overflow edge and pass from the vibrating screen into the discharge opening. For example, the overflow edge may have a height that is between 0.5 and 3 cm, e.g. B. about 1 cm. Air can be sucked in this way from top to bottom only through the vibrating screen, and each time when the filter cake lifts due to the vibrations in the short term from the vibrating screen.

With the proposed device, a high degree of separation can be achieved with high throughput, in that the solid constituents are finally present with the highest possible dry fraction, that is to say the smallest possible proportion of liquid contained therein. Alternatively, however, the device can be operated deliberately in such a way that solid constituents do not reach as high a level as possible Have dry fraction, but rather still liquid and thus present pumpable, if this should be advantageous for their further use. The degree of separation can therefore deliberately not be set to the maximum, and this is typically associated with an increase in throughput. For example, by appropriate design of the vibrating screen, the separation performance can be deliberately set low, so that a filter cake but rather a liquid from the vibrating screen enters the discharge, but in comparison to the supplied solid-liquid mixture has a higher proportion of solid components. For example, the permeability of the vibrating screen can be reduced by a smaller opening ratio, for example by using a perforated plate instead of a screen.

As solid constituents, the material is referred to, which leaves the vibrating screen in the conveying direction, passes into the discharge opening, and has a higher solids content than the device supplied solid-liquid mixture, and in particular a higher solids content than that sucked across the vibrating screen Material called liquid constituents.

The so-called solid constituents can therefore also be liquid, for example pumpable. In this case, it may typically be provided not to recirculate the solid constituents, for example to a slurry tank, but to a second tank, for example a tank, which is available stationary or as part of a tanker truck. The proposed device is used in this case to concentrate the solid-liquid mixture by using as so-called solid constituents a flowable material is provided which has a higher solids content than the originally present solid-liquid mixture. Slurry, for example, has an economic value that depends on the nutrient content, which in turn is determined in particular by the solids content. By the above-mentioned concentration with solids, the value of the solid components obtained, which can be applied as a pumpable liquid fertilizer, compared to the originally present solid-liquid mixture can be significantly increased.

Apart from the example of manure preparation, a device according to the proposal can also be used for the otherwise separate solid and liquid components. Using the example of liquid manure separation, first practical experiments have shown that the amount of solid components could be reduced by about 7 to 8% to significantly less than 1%.

To improve the performance of the device can be provided to allow a higher material throughput. For this purpose, a pipe (not shown in the drawings) may be oriented in a lying manner in the interior of the housing, above the inclined screen surface and inside the solid-liquid mixture, the pipe being made from the housing. The tube has apertures in its wall in the portion which is within the housing, similar to a drainage tube, so that liquid portion of the solid-liquid mixture can enter the tube. The tube is the same negative pressure, as prevails in the housing below the screen surface. Even if with the in the Tube entering liquid solids enter the tube, the performance of the entire device is significantly increased. Namely, the device is usually connected to a large reservoir of a solid-liquid mixture, and the liquid filtrate, which is withdrawn from the device is recirculated in this large reservoir, so that from this recycling only the solid is withdrawn exiting the device. Solid components that have passed into the mentioned pipe and return to the large storage tank will consequently be re-fed to the device sooner or later. If then already a large proportion of solids has been withdrawn from the solid-liquid mixture and the solid-liquid mixture flowing into the device contains a lower solids content, the probability is greater that the initially circulated solids now on enter the screen surface, are promoted above the liquid level also upwards, and are discharged in this way from the cycle as dry matter. The described measure for improving the performance thus serves to effect a higher throughput of the device, so it represents a quantitative improvement.

The improvement of the performance of the device can also be done in qualitative terms, namely by allowing the deposition of very small solid particles from the solid-liquid mixture, so the purity of the liquid filtrate is increased. In practical experiments, it has been found that sieve surfaces with a mesh size or pore size of 7 μιη can be used, which is an unusually high filtration fineness, which is accordingly a very Good quality of withdrawn from the solid-liquid mixture liquid - in many applications: water - allows. This qualitative improvement of the device can be made possible by the fact that the screen surface oscillates with a particularly high intensity. For example, a particularly high vibration frequency can be used. Taking into account the vibration frequency and the vibration amplitude which is exposed to the screen surface or which performs the screen surface, the vibration intensity can be expressed in g (gravitational acceleration). According to the proposal, the vibration intensity may have values of 7 g or more, in particular of 10 g or more, in particular, for example, values lying between 11 g and 13 g and with which good results have been achieved in practical experiments.

The qualitative improvement of the device can also be effected by the fact that the solid-liquid mixture is not only vibrated by the movements of the screen surface itself, but that it is subjected to ultrasound. For example, ultrasound can be directed from below against the sieve surface, so that the ultrasound acts on both the solid-liquid mixture and on the sieve surface.

The result of the qualitative improvement of the device is that deposits of solids are avoided in front of the pores of the screen, so that despite the mentioned filter fineness down to 7 μιη a blockage of the screen surface can be avoided. Another aspect of the developments of the known device relates to the aspect that the exiting from the device substances are sanitized so that they can be easily stored and / or transported. For example, the disposal of organic hospital waste, especially if they contain human excretions, can be highly problematic from a hygienic point of view, especially if in disasters or disease areas these excretions may contain germs that pose a health hazard. If, for example, in areas contaminated with MERS, AIDS or Ebola, such waste from hospitals or infirmaries reaches the normal sewage system - if there is any sewer system at all - and the germs contained in this waste can later escape to the atmosphere, this will be counteracted supports the efforts of the respective hospitals or infirmaries the uncontrolled spread of dangerous germs. On the one hand, this problem relates to regions in which there is typically no sewerage or clarification facilities for the disposal of organic waste, and relates to areas in which, for example, due to natural disasters, facilities such as sewers or clarifiers have been destroyed or rendered unusable, and this problem is concerned Finally, provisional settlements that are to be used only temporarily for a certain period of time, such as refugee camps, or settlements with shelters in disaster areas. But regardless of whether the organic waste in disease areas contain dangerous pathogens, this problem also affects the so-called civilized or highly developed Areas where there is a problem of multidrug-resistant bacteria. Also, such germs should not enter the environment uncontrolled as possible.

By means of a device according to the proposal, the organic wastes, which are obtained as a solid-liquid mixture, can be separated and sanitized. For example, while the sanitized liquid filtrate can be used for irrigation or easily drained into drains, the solids can be placed in a closed incinerator. Not only by the thermal utilization of the solids, the energy contained therein can be used, but by the combustion and harmful germs, which may be contained in the solids are reliably rendered harmless.

The sanitation can be carried out, for example, by irradiating the solid-liquid mixture and / or the liquid filtrate with UV light. Also, the solids can be irradiated with UV light, but there is the problem that this can only be a complementary measure, because probably the solids can not be completely penetrated by the UV radiation and sanitized accordingly. The sanitization may alternatively or additionally to UV irradiation be effected in that the solid-liquid mixture and / or the liquid filtrate and / or the deposited solid is heated by means of microwaves to a sanitation temperature, for example, above 70 ° C or 80 ° C can lie. The device may advantageously be provided with a post-treatment unit for the solid precipitated from the device. This post-treatment unit can be designed, for example, as a packaging device. For example, the solid can be pressed into bales, which are then mechanically wrapped with foil and wrapped airtight in this way. The bales can be designed, for example, in a manner known per se as round bales, or advantageously cuboid shaped, so that they can be stacked to save space. Or the solid can be filled into a foil tube, one end of which is closed, and clamped and sealed after filling a desired tube length, and optionally cut from a considerably longer, still unfilled tube, so that - as in the sausage production - Tube sections are created, which are closed at both ends and contain the solid. Both the bales mentioned and the aforementioned tube sections then enable the safe storage or the safe transport of the packed solid so that it can be transported, for example, to the mentioned incinerator. If the solid has a high - and possibly also because of its contained hazardous substances or germs - the thermal utilization in a closed incineration plant can be energetically advantageous while ensuring at the same time that organic ingredients of the solid are rendered harmless. Such closed incinerators (unlike open field fires) are typically equipped with powerful filters. so that any remaining, inorganic harmful particles can be rendered harmless, even beyond the thermal effect, and can not be released into the environment.

To the housing and the adjoining, so-called funnel into which the solid passes, can advantageously connect several pipes to be able to supply auxiliaries:

For example, sanitizing material may be added to the solid flowing through the funnel by means of a tubing adjoining the funnel. Or it may be added to the moisture-absorbing material, which influences the mechanical properties of the solid, for example, to better press it in the downstream aftertreatment unit or to allow improved dimensional stability of the pressed solid, such as the aforementioned bales.

A plurality of pipe connections is provided at the end of the device where the screen surface is located lowest, ie at the so-called inlet end, in the region of which the inlet openings are located. In addition, a lateral pipe is provided in the region of this inlet end, which opens into the housing above the screen surface. Through the pipe connections and the pipe, the mentioned auxiliaries or process auxiliaries can be guided into the housing. The fact that the pipeline is arranged higher than the pipe connections, the behavior or the effect of each supplied Stoffs be influenced. In addition, further pipelines or pipe connections can be provided in the conveying direction of the screen surface, so that even at a later time during the separation process within the housing substances the solid-liquid mixture can be added in its original composition or with increasing solids content. The arrangement of the screen surface is made clear by a double row of holes, which serves to fasten the screen surface and reveals the oblique course of the screen surface compared to the horizontal.

Through outlet lines, the liquid filtrate is withdrawn from the housing of the device.

The solids may either be packaged airtight, as discussed above, or they may be pressed at least so strong as to form a plug that seals the space enclosed by the housing and the funnel:

If, for reasons of health safety, no airtight coating of the solids is provided, a press screw may connect to the hopper as a post-processing device. The mentioned closed-walled pipe can be configured for this purpose as a transition piece, whose cross section passes from a rectangular to a circular contour, so that it can connect the press screw with a circular, tubular housing. At the end of the press screw, the harmless material into the Free enter and be dumped, for example, on the back of a vehicle or in the hold of a vehicle, or in place as a pile.

However, if an airtight wrapping of the solid is provided, it can be ensured by means of the mentioned, formed by the screw extruder, that in a subsequent portioning of the solids, for example to produce the aforementioned bales or to fill a film tube, no air from the outside into the Area of the device is possible in which a negative pressure to be maintained.

An embodiment of the invention will be described in more detail below with reference to the purely schematic representations. It shows

Fig. 1 is a perspective view of an apparatus for separating

manure;

FIG. 2 shows a view into a housing of the device of FIG. 1, together with a vibrating screen; FIG.

Fig. 3 is a perspective view in an open screw press the

Apparatus of Fig. 1;

Fig. 4 is a view from another perspective of the screw press of Fig. 3; a sectional cross-sectional view of the embodiment of Figure 1 in the region of a stepped screen surface of a vibrating screen and a pressure equalization between the space below the vibrating screen and the space above the vibrating screen. the detail A increases; in a single representation with a drivable by a motor rotary cutting unit, which is connectable to an inlet and an outlet in the liquid flow of the solid-liquid mixture as a second or single hydrodynamic reactor; in a side view (also in perspective) an embodiment nes hydrodynamic reactor with cooling fins and a magnetic rotating field and with ferromagnetic needles; a cross-sectional representation of the embodiment of FIG. 8 and partially broken embodiment of FIG. 8 with arrangement of the conductor loops with a 120 ° Wickelungsversatzmaß. In the drawings, a total of 1 denotes a device which serves for separating solid and liquid components of a solid-liquid mixture, in particular manure. The device 1 has two housing 2, which are combined to form a common module, in each of which a vibrating screen 3, which is inclined relative to the horizontal, is arranged. In the left or rear housing 2 in Fig. 1, an end wall 4 is mounted, which has been removed in the case of the right or the viewer towards 2. On the top of this assembly, so the two housing 2, a vibration drive 5 is mounted.

The device 1 is designed as a mobile device in the form of a truck trailer, with a frame 6, wheels 7 and a drawbar 8, which can be connected by means of a trailer hitch to a towing vehicle. About vibration damper in the form of elastomeric bearings 40, the housing 2 are decoupled from the frame 6 vibrationally.

This mobile device 1 is shown in Fig. 1 in front of a slurry tank 9. A corrugated tube 10 leads manure as a solid-liquid mixture from the slurry tank 9 to the device 1, namely a pump provided there 11. From the pump 11 from the solid-liquid mixture passes through a pipe 12 to the two housings 2, wherein the pipe 12 branches and leads to two inlets 14, each of which opens into one of the housing 2. The liquid components which pass through the vibrating screens 3 pass through outlets 15 from the housings 2. In this case, two outlets 15 are provided on the underside of each housing 2. The processes 15 open into a manifold 16, which is designed as a transverse square tube. From the collection tube 16, the liquid components are passed through a suction line 17 to a suction pump 18. From the suction pump 18 they pass through a return line 19, which is designed as a tube, back into the slurry tank. 9

The vibrating screens 3, and in the illustrated embodiment, the two housings 2, are arranged obliquely relative to the horizontal. 1, from left to right, so that the right end of a vibrating screen 3 is arranged higher than the left, lower end of the vibrating screen 3. The level of solid-liquid mixture within a housing 2 is set during operation of the device 1 so that the vibrating screen 3 protrudes with its front in the conveying direction, right end of the solid-liquid mixture upwards.

The solid components arrive on the vibrating screen 3 at the right end of the housing 2 and pass through a discharge opening into a funnel 20, which tapers downwards. In parallel operation of the two vibrating screens 3, namely, when the solid-liquid mixture is equally conducted through the pipe 12 in both housing 2, get from both housings 2, the solid components in the hopper 20 and from there down into a plenum 21st From the collecting space 21, the solid components are conveyed away by means of a screw conveyor 22. Due to the maximum permissible length that the device 1 may have as a vehicle trailer, the screw conveyor 22 is designed divisible and the end shown in Fig. 1 right represents a connection area. An extension piece 23 of the screw conveyor 22 can from there the screw conveyor 22 on the extend the illustrated right end to a greater length and to a greater height. In the illustrated embodiment, a foldable or foldable configuration of the screw conveyor 22 is provided, wherein the extension piece 23 is always hingedly connected to an upright axis hingedly connected to the fixed part of the screw conveyor 22 and can be pivoted from its illustrated folding position into an extension position in which it extends this fixed part of the screw conveyor 22 rectilinear. Of the screw conveyor 22 including the extension piece 23 is shown in Fig. 1, only the outer cladding tube, the actual screw runs in a conventional manner within this cladding tube.

Fig. 2 shows a view into the right and front housing 2 of the device 1 of Fig. 1, in which the end wall 4 is removed. The pipeline 12 extends in the region of the inlet 14 into the housing 2. On the housing 2, a guide sleeve 24 is provided, through which the pipe 12 extends, so that in this way the pipe 12 is decoupled from the housing 2 in terms of vibration and can remain relatively rigid, while the housing 2 together with the vibrating screen 3 through the Vibration drive 5 is vibrated. An air inlet into the housing 2 is firstly possibly possible through an annular gap, which results between the guide nozzle 24 and the thinner pipe 12 there, provided that this annular gap should not be sealed, but this can be advantageously provided in a conventional manner. Secondly - and optionally as the only place - an air inlet in the discharge opening is possible, namely where the hopper 20 connects to the housing 2. Incidentally, the housing 2 is closed. The mentioned admission of air occurs due to the suction effect of the suction pump 18, which generates a negative pressure in the housing 2.

An overflow edge 38 is provided in the conveying direction at the front of the vibrating screen 3, in front of the discharge opening, so that the solid components accumulate on the vibrating screen 3 and have to reach a corresponding height or layer thickness before they can overcome the overflow edge 38 and reach the discharge opening.

Below the inlet 14, a manifold 25 is provided, which is designed as a flat sheet, which extends substantially transversely below the inlet 14 and which has a plurality of distribution ribs 26, which passes through the inlet 14 into the housing 2 solid-liquid mixture distribute over the entire width of the vibrating screen 3.

While in the case 2, the viewer front end wall 4 is removed and the view of the vibrating screen 3 and the distributor 25 is free, from Fig. 2, an end wall 39 can be seen, which is opposite the remote end wall 4, and in the Comparison to the end wall 4 lying flat and above the funnel 20 is arranged.

Fig. 3 shows a possibility, as in the illustrated embodiment, the collecting chamber 21 may be configured: From the hopper 20 enter the solid components of the solid-liquid mixture from the housing 2 into the plenum 21. The plenum 21 is open at the bottom Housing designed in which a screw press 27 runs. Also in this case, the actual screw, namely the pressing screw, not visible, but rather a filter 28 can be seen.

4 schematically shows the structure of the screw press 27. The filter 28 is formed by a multiplicity of flat iron 35 which extend in the longitudinal direction of the screw press 27 and which are in each case combined to form packages 29.

Each package 29 in this case has a plurality of upright flat iron 35, for example, between two and ten pieces, purely by way of example in the illustrated embodiment, four flat bars 35 form a packet 29. The packages 29 are arranged so that they abut each other with their radially inner longitudinal edges, while between two adjacent packages 29 at the radially outer periphery of the filter 28 each have a gap in the longitudinal direction of the screw press 27, since the flat iron 35 within a package 29 parallel and each other arranged over the entire surface. Spacers 36 are provided between the individual packages 29.

The packages 29 surround a press screw 37 similar to a longitudinally slotted cladding tube. In Fig. 4, the filter 28 is adjacent almost to the outer periphery of a press screw, but a small gap between the filter 28 and the press screw 37 is provided to allow a low-wear operation of the screw press 27. Notwithstanding this embodiment, a significantly larger gap between the filter 28 and the press screw 37 may be provided, if this should be advantageous for the treatment of the respective material to be processed.

The front in the conveying direction, shown in Fig. 3 left end of the screw press 27 is closed by a plug 30, which is guided by means of a bolt 31 in an abutment 32. At the abutment 32, a compression spring 33 is supported, which holds the plug 30 in its closed position, in which it abuts the front end of a cladding tube 34, which surrounds the press screw 37 following the filter 28.

When the screw press 27 is put into operation, the plug 30 first abuts the cladding tube 34 and closes it. By the pressing pressure, which builds up inside the screw press 27 by the rotation of the press screw 37, moisture is expelled from the solid components and through the filter 28th pressed. Upon reaching a sufficiently high pressing pressure, the compressed solid components can press the plug 30 against the action of the compression spring 33 from the cladding tube 34, so that now the separated material, namely the solid components, from the annular gap between the plug 30 and the cladding 34th exit and fall down. There they are detected by the screw conveyor 22.

As an alternative to the described embodiment, it may be provided to design the collecting space 21 simply as a container, that is to say as an empty space without a screw press 27 mounted therein. The screw press 27 can in this case be operated as a separate device, for example only if necessary, if the first place by means of of the vibrating screen 3 separated solid components should have an even higher solids or dry content. For example, in this case, the material can be conveyed by the screw conveyor 22 from the collecting space 21 to the screw press 27. Depending on the type of further processing, the separated solid components are provided, a post-treatment of the coming of the vibrating screen 3 solid components by means of the screw press 27 can be done or omitted.

5 shows in a cross-sectional view the vibrating screen 3 in a design with two vibrating screen sections 3.1 and 3.2 in the conveying direction, which are stepped, so that between the vibrating screen sections 3.1 and 3.2 there is a breaking edge 3.3 and the surface of the vibrating screen section Ches 3.2 extends with a vertical distance to the surface of Schwingsiebbereiches 3.1 and lower overall. This leads to the fact that during the promotion of solid-liquid mixture in the conveying direction in the field of Abtreppung and thus in the fracture edge it comes to a turning process in the sense of overhead turning of the discontinued liquid-solid material, so that the first top Material now comes to lie below the upper surface directly on the screen surface of the second Siebflächenbereiches 3.2, whereby the degree of separation is further favored.

In addition, it comes between the lower housing space 2.1 and the upper housing chamber 2.2 to a pressure equalization according to the direction of the arrow P in Fig. 6, since by the rubber lip GL in Fig. 6, a pressure equalization between these two spaces can be done automatically. Due to the elasticity of the rubber lip, this pressure equalization can take place by these lifts and allows air circulation due to the opening provided there. This prevents the meshes of the screen surfaces of the vibrating screen from becoming clogged and thus always ensuring that a functioning operation is present during the separation process.

FIG. 7 shows an exemplary embodiment of a hydrodynamic reactor in the form of a cutting mechanism 40, which is driven by a motor 41 and has cutting blades 42 with a corresponding counter-blade 43. The cutting blades 42 are rotated by the motor 41 in rotation. Via the connecting pipe 44, a liquid to be purified is supplied, wherein solid particles can collect in the pipe region 45. After appropriate diversion The cutting blades 42 process the liquid to be purified, which in turn flows out of the reactor 50 via the outlet 46 for further treatment if necessary.

In Fig. 8, another hydrodynamic reactor is shown in the form of a reactor 50 to be provided with an electromagnetic rotating field of the inlet opening 51 and an outlet 52 and has an inner chamber 53 (Fig. 9 and 10) in the magnetizable needles 54 and Blades 54 are arranged. This inner reaction space 53 is provided with a winding of electric wires 55 connected to a power source 56. In addition, cooling fins 57 are provided on the outer jacket. Bypass lines 58 and 59 are also provided.

As can be seen in more detail in FIG. 10, the conductor loops of the winding of the conductors 55 are provided such that an angle α of 120 ° exists between the inlet and the outlet on the outer circumference of the reaction chamber 55. Thus come per 160 ° in each case three inlets and three outlets, so that it can be accomplished that the magnetizable needles or cutting 54 so circled within the reaction chamber that they work in orderly alignment as a rotating ring in the chamber 53, which is quite achieve excellent results in the liquid.

Claims

claims

1. A process for the purification and / or sterilization of liquid and / or aqueous media comprising the following process steps:

- Cavitation treatment of the medium, in particular with Strahlkavitation, at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar;

- Subsequent treatment of the medium in a hydrodynamic reactor with a magnetic rotating field and magnetic and / or magnetizable elements, in particular with ferromagnetic needles and / or with a rotating cutter with rotating cutting blades at a negative pressure of <1 bar, preferably 0.3 to 0.7 bar;

- Subsequent deposition, in particular sedimentation of the treated medium with a sludge separation at a reduced pressure of <1 bar, preferably 0.3 to 0.7 bar.

2. The method according to claim 1, characterized in that the treatment with jet cavitation in the hydrodynamic reactor to form strong Oxidati- onsmitteln OH, H2O2 and O3 is performed.

3. The method according to claim 1 or 2, characterized in that the treatment is carried out in the hydrodynamic reactor with dispersing of particles up to Submik- rondimensionen and enlargement of the phase interface gas-liquid-solid.

4. The method according to any one of the preceding claims, characterized in that an adjustment of the aqueous medium takes place before the cavitation treatment.

5. The method according to any one of the preceding claims, characterized in that in the course of treatment in the hydrodynamic reactor at least one reagent is added, which is to be selected from the following group: milk of lime, aluminum sulfate and / or iron chloride.

6. The method according to any one of the preceding claims, characterized in that the recovered medium is additionally treated in a rotating pulse device.

7. The method according to any one of the preceding claims, characterized in that the medium is additionally filtered in a Tiefbettfilter.

8. The method according to any one of the preceding claims, characterized in that the medium is additionally ozonized.

9. The method according to any one of the preceding claims, characterized in that the medium is treated with a UV radiation.

10. The method according to any one of the preceding claims, characterized in that the method for the treatment of liquid and aqueous media is preceded by a further process in which solid and liquid components of a solid-liquid mixture are separated, wherein the solid-liquid Mixture via an inlet (14) arranged in a substantially closed housing (2), a vibrating screen (3) having vibration conveyor is given and within the housing in a space above and below the vibrating screen relative to the ambient pressure of the housing negative pressure ( Negative pressure) is generated, and wherein within the housing (2) in the space (2.1) below the vibrating screen (3) a relation to the ambient pressure negative pressure (negative pressure) is applied as in the space (2.2) above the vibrating screen.

11. The method according to claim 10, characterized in that within the housing (2) in the space (2.1) below the vibrating screen (3) and in the space (2.2) above the vibrating screen (3) a negative pressure of <1 bar, preferably 0.3 to 0.7 bar is applied.

12. The method according to claim 11, characterized in that within the housing (2) in the space (2.1) below the vibrating screen (3) a negative pressure of (-0.3) bar to (-0.8) bar and in the space above the vibrating screen (3) a negative pressure of -0.2 to -0.6 bar is applied.

13. The method according to any one of claims 10 to 12, characterized in that between the space (2.1) below the vibrating screen (3) and the space (2.2) above the vibrating screen (3), a pressure compensation is performed.

14. The method according to claim 13, characterized in that the implementation of the pressure compensation takes place automatically.

15. The method according to any one of claims 13 or 14, characterized in that the pressure equalization takes place at the end portion of the vibrating screen (3) in the housing (2), which is arranged opposite the region of the vibrating screen (3) on which the solid Liquid mixture is given to the vibrating screen (3).

16. The method according to any one of claims 13 to 15, characterized in that the level of the solid-liquid mixture is set so high that the vibrating screen (3) partially protrudes above this level up and that the pressure compensation is performed in the area in which the vibrating screen (3) protrudes above this level.

17. The method according to any one of claims 10 to 16, characterized in that the solid-liquid mixture through the vibrating screen (3) is promoted such that it undergoes a turning operation in the course of the conveying movement.

18. The method according to claim 17, characterized in that the solid-liquid mixture in the course of its conveying movement on the vibrating screen (3) performs an overhead movement.

19. The method according to any one of claims 10 to 18, characterized in that the oscillation of the vibrating screen (3) is set such that the solid-liquid mixture is held during the Separiervorgangs in a kind of floating state above the vibrating vibrating screen (3).

20. The method according to any one of claims 10 to 19, characterized in that the solid constituents are fed after the Separiervorgang Nachbehanidung in the form of a hydrothermal carbonization.

21. The method according to any one of claims 10 to 20, characterized in that the solid-liquid mixture and / or the separated solid portions and / or the dissipated separated liquid is subjected to a UV treatment and / or an ultrasonic treatment.

22. The method according to any one of claims 10 to 21, characterized in that in the housing (2) below and / or above the vibrating screen (3) prevailing negative pressure detected by pressure transducers and the detected measured values are fed to a measured value processing device and in dependence of the measured value result at least one pressure generator is controlled in order to set process-specific pressure parameters according to the process parameters.

23. Device for carrying out the method according to one of claims 1 to 9.

24. An apparatus for sterilizing and purifying aqueous media, and in particular for carrying out a method according to one of claims 1 to 9, the apparatus comprising:

- A specially designed as Strahlkavitator cavitator, which is equipped with elements for injection of air or oxygen-air mixture;

a hydrodynamic reactor with a magnetic rotating field and with magnetic and / or magnetizable elements, in particular with ferromagnetic needles;

a unit for separation, in particular for sedimentation, preferably combined with a sludge separation device;

25. The apparatus according to claim 24, characterized in that it is additionally equipped with a compensation mixer, which is installed in the flow direction in front of the Strahlkavitator.

26. Device according to claims 10 or 11, characterized in that in addition a device for metering reagents for the hydrodynamic reactor is provided.

27. Device according to one of claims 24 to 26, characterized in that the unit for sedimentation of the medium is provided with hydrocyclones.

28. Device according to one of claims 24 to 27, characterized in that in addition a rotating pulse device is provided, which is installed in the flow direction after the unit for sedimentation.

29. Device according to one of claims 24 to 28, characterized in that in addition Tiefbettfilter are provided, which are installed in the flow direction after the unit for sedimentation.

30. Device according to one of claims 24 to 29, characterized in that in addition a unit is provided for the ozonization of the medium, which is installed in the flow direction after the unit for sedimentation.

31. Device according to one of claims 24 to 30, characterized in that in addition a unit for UV irradiation of the medium is provided, which is installed in the flow direction after the unit for sedimentation.

32. Device according to one of claims 24 to 31, characterized in that in addition an automatic control unit for controlling the processes is provided.

33. Device according to one of claims 24 to 31, characterized in that the hydrodynamic reactor is equipped with such a rotating magnetic field via electrical conductors having in the 120 ° pattern (inlet / outlet) conductor loops.