DE102015106823A1 - Modular system and method for flexible deferrisation of water - Google Patents

Abstract

The invention relates to a modular system for the flexible defrosting of water, comprising - a first module (1) with one or more parallel or in series containers (3) containing at least one reaction tank (2) with several aerators (6), whose principle of operation is based on the principle of a mammoth pump (6) or an ejector, of which at least one aerator (6) is connected to an aerator attachment (8) for introducing a solid into the reaction basin (2), - a second module (11) with one or more a plurality of containers (14) arranged in parallel or in series, each containing at least one injection tank (12) for the injection of a flocculation aid and at least one flocculation basin (13) for iron hydroxide floc to be deposited, - a third module (21) having one or more in parallel or in series arranged containers (23), each containing at least one sedimentation tank (22) for the sedimentation of Eisenhydroxidfloc ken and a clear water withdrawal device (27). Furthermore, the invention relates to a method for the flexible deferrisation of water in a corresponding modular system. The main advantage of the method according to the invention is that it combines the previously independent according to the prior art process steps of venting, the mixing of neutralizing agents and the entry of kinetic energy for self-purification of the reaction tank together.

Description

The invention relates to a modular system and method for flexible defrosting of water using novel venting and blending devices.

The modular system is used for decentralized treatment of iron-contaminated waters. The use is in the treatment of waters with a large variation in the iron concentration of 5 to 1500 mg / l, the volume flow of 5 to 500 l / s and the oxygen demand of 0 to 230 mg / l. The device is suitable both for highly concentrated waters with high oxygen demand and for low-concentration waters with low oxygen demand. These waters are usually treated with conventional defrosting systems only with a very high level of technical equipment.

Using the example of the lignite mining area of Lusatia, it can be stated that, in particular, waters contaminated with iron represent a great potential for the pollution of surface waters due to their areal occurrence when passing into the receiving waters. The iron-rich waters leak out at locations or can be found in locations that are largely infrastructurally poorly developed. Traditionally, the waters would be collected, taken to a central stationary water treatment and treated there. Due to the spatially distributed occurrence of such waters, this solution is not feasible without major cuts in uses, ownership and infrastructure.

The variability of the volume flows and characteristics of the water to be treated is also very wide. In addition, the occurrence of such waters in space and time as well as in terms of volume flow and consistency characteristics is difficult to predict. Therefore, a solution is required that saves space, has low requirements for the subsoil and infrastructure and is flexible in terms of input values.

According to the prior art, stationary de-ironing water treatment plants include the process steps of aeration, mixing in of flocculants and flocculants, introduction of kinetic energy and sedimentation in dissolved process steps. The execution takes place as fixed installations, which are usually built with basins made of reinforced concrete in different sizes and shapes.

Conventional water treatment plants are stationary structures. These are designed with regard to the quality and quantity of the water to be treated as well as the treatment goals. Within defined spans, these systems rely on constant inflow conditions. A stronger change in the influx forces us to make complex adjustments and to rebuild or dismantle the plant. Compared to modular systems, conventional water treatment plants are severely limited in their flexibility and mobility.

The state of the art already offers solutions for mobile water treatment plants. The mobility and the associated flexibility of such water treatment systems is achieved by installing the entire system in a container in the form of a compact system. Many providers use standard shipping containers. Some of these solutions are also flexible in the design of individual components of the system dar. Such are compact sewage treatment plants with a variable chamber system within the container, which also from the DE 295 02 118 U1 or the AU 002011274292 A1 are already established. The treatment steps or components of the water treatment are here adapted according to the requirements of the performance or even completely replaced. The main drawback of these compact systems is their considerable capacitive limitation, both in terms of input values and throughput. Since the compact systems within a container several process steps are installed in the form of different components, a treatment for the above application in terms of capacity meets with technical and economic limits.

For the purposes of the invention, the necessary process steps for a flexible water treatment are removed from the scope of the individual standard container in order to cooperate in several, differentiated designed building blocks. This makes it possible to implement an adaptation to variable requirements using the modular modular principle.

Such an approach is already out of the DE 198 34 727 A1 this is suitable for the construction of pilot plants for water treatment only on a laboratory scale. Here, separate units were built for each component of the water purification process, which were modularly assembled as a test setup for a planned treatment plant in the laboratory for testing purposes. These Pilot plant is only designed for a throughput of up to 10 ml / min and can not be converted into a remediation-relevant system by scaling up.

Disadvantages of stationary water treatment plants are the very high approval, constructive and financial costs for the construction as well as the technical design to a narrow range with regard to the iron concentration, the volume flow and the oxygen demand. Another significant disadvantage is the possibly high expenses for adaptation under changed boundary conditions.

Modular systems for the treatment of iron-containing waters on the basis of standard containers are usually constructed "monolithic", that is, a container contains the equipment for all or for the essential steps in the treatment of water. The incorporation of several process steps in a container with specified dimensions limits its treatment capacity, whereby the use on a larger scale is technically and economically limited. In order to increase the capacity of such "monolithic" plants, several containers would have to be operated in parallel. Here, all process steps are to be operated in parallel. The design, ie the number of containers, inevitably depends on the limiting process step. This in turn implies that most of the process steps are oversized, making the overall process inefficient.

The object of the invention is to provide a defrosting system which is flexible in terms of iron concentration, location and time of use.

The object of the invention is achieved by a modular system for de-ironing water according to claim 1. Further developments are specified in the dependent claims.

• • ein erstes Modul mit einem oder mehreren parallel oder in Reihe angeordneten Containern, enthaltend jeweils mindestens ein Reaktionsbecken mit mehreren Belüftern, deren Funktion auf dem Prinzip einer Mammutpumpe oder eines Ejektors beruht, wovon mindestens ein Belüfter einen Belüfteraufsatz für das Einbringen eines pulverförmigen Feststoffs in das Reaktionsbecken aufweist,
• • ein zweites Modul mit einem oder mehreren parallel oder in Reihe angeordneten Containern, enthaltend jeweils mindestens ein Injektionsbecken für die Injektion eines Flockungshilfsmittels und mindestens ein Flockenreifebecken für abzusetzende Eisenhydroxidflocken sowie
• • ein drittes Modul mit einem oder mehreren parallel oder in Reihe angeordneten Containern, enthaltend jeweils mindestens ein Sedimentationsbecken für die Sedimentation von Eisenhydroxidflocken und eine Klarwasserabzugseinrichtung.

According to the invention, the modular system for de-ironing water

• A first module with one or more containers arranged in parallel or in series, each containing at least one reaction tank with a plurality of aerators whose function is based on the principle of a mammoth pump or an ejector, of which at least one aerator comprises a aerator attachment for introducing a pulverulent solid into the aerator Having reaction tanks,
• A second module with one or more containers arranged in parallel or in series, each containing at least one injection basin for the injection of a flocculation aid and at least one flocculation basin for iron hydroxide flakes to be deposited, and
• A third module with one or more containers arranged in parallel or in series, each containing at least one sedimentation basin for the sedimentation of iron hydroxide flakes and a clear water outlet.

The flexible deferrisation modular system of the present invention takes advantage of the prior art systems described above and implements a new, extended approach to treatment. The necessary treatment steps are carried out in differently equipped standard containers. The differentiated equipment of these containers enables the maximum adaptability of each treatment step to the respective inflow conditions. The highly efficient individual components are combined with each other in modular design in variable repetition numbers. For example, if more ventilation power is needed, the number of containers with aeration devices can be increased while, for example, the number of sedimentation containers remains unchanged as needed.

With the modular system of the flexible deferrisation device, iron-contaminated waters are treatable in a wide range of input values. The modular design of the water treatment plant also allows a relatively simple adaptation to temporarily changing requirements in terms of quantity and quality of the water to be treated. In addition, the modular design allows adaptation to a range of site conditions, allowing the plant to be used flexibly and repeatedly deployed at multiple sites.

With such a modularly expandable system, site-adapted defrosting systems are to be constructed in such a way that quickly usable plant systems with high efficiency can be created with minimum construction effort.

• – eine Anwendbarkeit für eine große Bandbreite der Eisenkonzentration, des Volumenstroms und des Sauerstoffbedarfs,
• – eine Flexibilität hinsichtlich des örtlichen und zeitlichen Einsatzes,
• – eine kurzfristige Verfügbarkeit infolge des hohen Vorfertigkeitsgrades der Module,
• – eine Minimierung der Baukosten der Container im Vergleich zu herkömmlichen Anlagen,
• – eine kompakte Bauweise,
• – geringe Anforderungen an die Infrastruktur und
• – ein geringerer Aufwand für die Genehmigung.

Decisive advantages of the invention are:

• An applicability for a wide range of iron concentration, volume flow and oxygen demand,
• - a flexibility in terms of local and temporal use,
• - a short-term availability due to the high degree of prefabrication of the modules,
• - a minimization of the construction costs of the containers compared to conventional systems,
• - a compact design,
• - low demands on the infrastructure and
• - less effort for approval.

• • Bereitstellung der erforderlichen Luft für den Oxidationsprozess,
• • Durchmischung des Wassers mit Neutralisationsmitteln und die
• • Selbstreinigung des Reaktionsbeckens.

The arrangement of the mammoth pumps or the ejectors in the container of the first module makes it possible to operate the following method steps in parallel:

• Providing the required air for the oxidation process,
• • mixing the water with neutralizing agents and the
• • Self-cleaning of the reaction tank.

The use of mammoth pumps or ejectors simultaneously brings about the saving of the otherwise usual for the entry of powdery solids disperser, separate ventilation equipment and agitators.

According to an advantageous development of the invention, the modular system additionally contains a fourth module for treating sludge withdrawn from the sedimentation basin of the third module via a sludge removal device, the sludge treatment being able to take place in the form of sludge thickening and / or sludge dewatering.

According to a preferred embodiment of the invention, in the second module, the injection basin for injection of a flocculation aid, preferably a polymer, is provided as a first basin, the injection basin having a vertical paddle mill for the mixing of the injected flocculation aid. Advantageously, a ripening basin for the growth of the iron flakes to be deposited is provided in the second module for growing the iron flakes to be deposited, in which a horizontal paddling plant for providing the necessary kinetic energy for flocculation and for non-destructive lifting of the grown flakes is arranged in a transfer line for sedimentation.

According to a further advantageous embodiment of the modular system according to the invention lamellar separators (plate) are arranged in an oblique position in the third module in the sedimentation tank for efficient deposition. Clear water drainage takes place, for example, via tooth-shaped sleepers and a sludge discharge preferably via pipe systems located below as a sludge removal device. For a sufficient iron separation, in particular for short residence times in the sedimentation basin, sludge recycling, preferably into the flocculation tank, can be advantageously established.

Compared to a conventionally constructed water treatment plant, the modular system of the device according to the invention advantageously requires a comparatively small amount of construction, space and licensing requirements for the construction, in the case of need necessary capacity adjustment as well as in the implementation or the dismantling of the plant.

• a) das eisenreiche Wasser zur Enteisenung in einem ersten Modul über einen Zulauf in ein Reaktionsbecken eingeleitet wird und im Reaktionsbecken mindestens ein Neutralisationsmittel zur pH-Wertanhebung über mindestens einen Belüfter, dessen Funktionsprinzip auf dem Prinzip einer Mammutpumpe oder eines Ejektors beruht und der mit einem Belüfteraufsatz für das Einbringen eines Feststoffs in das Reaktionsbecken verbunden ist, eingebracht wird, während gleichzeitig Sauerstoff über diesen und gegebenenfalls andere Belüfter in das Wasser des Reaktionsbeckens eingetragen wird,
• b) eine Flockung von bereits kolloidal suspendiert vorliegendem Eisenhydroxid und anderen Feststoffen im durch Verfahrensschritt a) behandelten Wasser im zweiten Modul durch Injektion von Flockungshilfsmitteln in einem Injektionsbecken und anschließend die Reifung der abzusetzenden Eisenhydroxidflocken in einem Flockenreifebecken erfolgt und
• c) die Sedimentation der Eisenflocken in einem oder mehreren parallel betriebenen Containern in einem dritten Modul erfolgt und das überstehende Klarwasser durch eine Klarwasserabzugseinrichtung einer Klarwasserablaufleitung zugeführt wird.

The inventive modular system, a method is possible in which

• a) the iron-rich water for ironing in a first module is introduced via an inlet into a reaction tank and in the reaction tank at least one neutralizing agent for raising the pH above at least one aerator whose principle is based on the principle of a mammoth pump or an ejector and with a Belüfteraufsatz is introduced for the introduction of a solid in the reaction tank is introduced, while at the same time oxygen is introduced via this and optionally other aerators in the water of the reaction tank,
• b) a flocculation of existing colloidally suspended iron hydroxide and other solids in the treated by process step a) water in the second module by injection of flocculants in an injection tank and then the maturation of the deposited Eisenhydroxidflocken takes place in a Flockenreifebecken and
• c) the sedimentation of the iron flakes takes place in one or more parallel operated containers in a third module and the supernatant clear water is fed through a clear water withdrawal device a clear water drain line.

Advantageously, the neutralizing agent enters the reaction tank as a suspension via an aerator outlet of the aerator provided with the aerator attachment.

An essential advantage of the modular system according to the invention is the possibility of a novel method which combines the previously independent according to the prior art process steps of venting, the mixing of neutralizing agents and the entry of kinetic energy for self-purification of the reaction pool. The combination of the three process steps in one causes a very efficient treatment while allowing the execution in the relatively limited dimensions of commercial containers.

Further details, features and advantages of embodiments of the invention will become apparent from the following description of exemplary embodiments with reference to the accompanying drawings. Show it:

1 : a first module with a reaction tank,

2 a second module with a flocculant aid injection and a ripening basin,

3 a third module with at least one sedimentation basin,

4 a modular apparatus in the form of a two-way water treatment plant and

5 : a modular water treatment plant for the iron removal of low-oxygen, medium-iron polluted groundwater, which is extracted via wells.

The 1 schematically shows a first module 1 with a reaction tank 2 in a large container 3 , The container 3 is designed as a mobile Abrollcontainer. The 1 shows in Figure a) a longitudinal section of the container 3 along the plane AA, in Figure b) a rear view and in Figure c) a plan view. In the reaction tank 2 opens an inflow 4 for the iron-rich water 5 , where the inlet 4 according to the in 1 shown embodiment from above over the short leg of an inverted J-shaped inlet pipe 4 that does not happen in the water 5a of the reaction tank 2 dips and thus above the liquid level 5b of the reaction tank ends. In the reaction tank 2 are as central components of the container 3 several aerators 6 (Aerator) according to the principle of the mammoth pump 6 built-in. Under mammoth pump 6 is a perpendicular to a liquid, in this case the iron-rich water 5a , immersed, preferably inverted U-shaped tube 6 to understand, in the below the liquid level 5b a gas, in this case air, by means of an in 1 not shown compressor (compressor) is pressed or injected by means of a blower, not shown.

The iron-rich water 5 is used for iron removal after removal and quantity measurement in the reaction tank 2 over the inlet 4 initiated. The air is over the lower area, the Belüfterfuß 6a the mammoth pump 6 pressed. By the rising of the air bubbles in the tube of the mammoth pump 6 Water is pumped and then, after moving up and down, it finally exits at the aerator outlet 6b in the bottom area of the reaction tank 2 out. About not shown screw conveyor, for example, lime hydrate 7 as a neutralizing agent 7 or flocculant 7 also via the special mammoth pumps 6 into the water 5a of the reaction tank 2 brought in. This is at least one of the area above the water level 5b to the aerator foot 6a the mammoth pump 6 reaching aerator tower 8th with the aerator foot 6a the mammoth pump 6 connected. The neutralizing agent 7 passes through the hopper, not shown, via a funnel 9 in the aerator attachment 8th , where at the essay entrance 8a , which is formed wider than the rest of essay 8th and in the area of the water level 5b located, openings for the discharge of water 5 from the reaction tank 2 in the essay 8th into it. The neutralizing agent 7 gets along with the water 5 to the aerator foot 6a the mammoth pump 6 and with the help of the rising air bubbles as a suspension through a not shown aerator outlet into the water 5a of the reaction tank 2 , The further mixing is due to the diffuser outlets oriented in different directions 6b promoted.

• • Bereitstellung der erforderlichen Luft für den Oxidationsprozess,
• • Durchmischung des Wassers 5a mit Neutralisationsmitteln 7 und
• • Selbstreinigung des Reaktionsbeckens 2.

The arrangement of the mammoth pumps 6 in the reaction tank 2 allows you to operate the following process steps in parallel and in the smallest of spaces:

• Providing the required air for the oxidation process,
• • mixing of the water 5a with neutralizing agents 7 and
• • Self-cleaning of the reaction tank 2 ,

The use of mammoth pumps 6 or of ejectors, the saving of the otherwise usual for the entry of powdery solids disperser, separate ventilation equipment and agitators.

In the lower part, which means in any case below the water level 5b , is a process 10 for that in the reaction tank 2 treated water 5a arranged over which the water 5a can get into the next module.

In place of mammoth pumps 6 Ejectors can also be used. Ejectors are a type of jet pump and generate a vacuum according to the venturi principle. This negative pressure is the interference of the neutralizing agent 7 or for producing a suspension of neutralizing agent 7 and water 5a in the reaction tank 2 used.

The reactions in the reaction tank (s) 2 of the first module 1 subsequent steps in a second module 11 instead, which comprises one or more containers, each with an injection tank for the addition of flocculants and with one or more flocculation troughs. Such a second module 11 is in 2 shown schematically. Figure a) 2 shows the second module 11 as a longitudinal sectional view in the plane AA, the figure b) is a rear view and the figure c) is a plan view. The second module comprises according to the schematic representation in FIG 2 an injection basin 12 and a flocculation riparian pool 13 in the same container 14 that as a roll-off container 14 is trained. In the first basin, the injection basin 12 with a horizontal supply line 15 for the water treated in the reaction tank in the area of the bottom of the injection basin 12 , the flocculant FHM, for example a polymer, is injected and by means of a vertical paddle mill 16 that is a paddling plant 16 with vertical axis 16a , mixed in.

In the downstream ripening basin 13 into which the treated water 5a from the injection basin 12 through one below the water level 5b positioned transfer opening 17 over one between the wall of the transfer opening 17 and an opposite baffle 18 passed vertical deflecting channel, grow the deposited iron flakes on a defined minimum size zoom. A horizontal paddling work contributes to this 19 that is a paddling plant 19 with horizontal axis 19a , the necessary kinetic energy for flocculation and lifts, as in 2 represented by a curved arrow, the grown flakes non-destructive in a transition 20 for subsequent sedimentation. The prerequisite for the sedimentation at economically meaningful residence times is the formation of a minimum size of the flakes and their non-destructive transfer into the sedimentation basin. The gentle transfer of the grown flakes contributes to the efficiency of the flocculants use and to reducing the residence time of the water 5a in the sedimentation at.

The sedimentation of the iron flakes takes place in a third module 21 comprising one or more parallel operated containers each having at least one sedimentation basin. The 3 shows a third module 21 as a longitudinal sectional view of the plane AA in Figure a) as a rear view in Figure b) and as a top view in Figure c). The third module 21 includes a sedimentation basin 22 in a container 23 that as a roll-off container 23 is trained. The solids-laden water to be treated 5a passes through an inlet 24 standing in the area below the water level 5b is positioned in the sedimentation basin 22 , For efficient separation, lamella separators are used 25 (Slab separator) in inclined installation use. The clear water discharge takes place in the upper area at the rear end of the sedimentation basin 22 in one or more clear water drainage pipes 26 , According to 3 the clear water discharge takes place in two clear water drainage pipes 26 , which are merged in the course to a clear water drain line. The clear water drain into the clear water drainage pipes 26 via a clear water drainage channel, preferably a clear water drainage channel with dental sleepers 27 at the top of the sedimentation basin 22 speak in the area of the water level 5b ,

The sludge removal takes place in the sedimentation basin 22 below lying pipe systems 28 , For a sufficient Eisenhydroxidabscheidung, especially for short residence times in the sedimentation tank 22 , may be necessary, an in 3 not shown additional sludge return into the ripening 13 to install.

The treatment of the sedimentation tank 22 withdrawn sludge can be done in a fourth module, not shown by Schlammeindickung and sludge dewatering.

First exemplary embodiment: Design of a two-volume container-supported water treatment plant for a volume flow of 25 l / s

In the reorganization mining of the Lusatian lignite mining area, groundwater recharge in some running waters leads to the discharge of highly ferrous groundwater. This phenomenon is known u. a. as "brown Spree" in the area of Spremberg. The objective is to significantly reduce the iron load in the Spree by intercepting local, heavily ferriferous inflows and their treatment.

In a local drainage ditch, groundwater with 350 mg / l of iron predominantly emerges as reduced iron and flows untreated into the Spree. The iron-rich water of the ditch represents a local stress center, which contributes significantly to the iron deposits in the Spree. By local water treatment, the iron load in the drainage ditch should be reduced by at least 90%. In the water treatment plant to be built 90 m ³ / h or 25 l / s iron-containing water to be cleaned.

The specific lime requirement as Ca (OH) _{2 is} approximately 460 mg / l. With an efficiency of 80%, the hydrated lime requirement is calculated at 1.3 tonnes per day. The stoichiometric oxygen demand for the oxidation of the iron is about 50 mg / l. This results in a requirement of 108 kg / d oxygen for oxidation. With an estimated aerator material input efficiency of 20% and a depth-dependent oxygen transfer rate of 6 g / m ³ / m, the air requirement is about 2,000 m ³ / d.

The solution is in the example case, as in 4 shown schematically, implemented:
The water is from a lockable extraction structure 29 , which is designed as a reinforced concrete shaft, taken over pumps in duplicate. The extraction shaft 29 is connected to the existing grinding wells of the drainage trench with an 8 m long polyethylene pipe. The discharge shaft is followed by a measuring shaft with a magnetic-inductive flowmeter (MID).

The aeration and metering of the neutralizing agent acting as flocculant takes place in the first module 1 in two reaction tanks 2 in the execution as a road transportable container of 2 × 40 m ³ total volume with a useful volume of approximately 35 m ³ . Two blower stations 30 with a capacity of 2 × 160 m ³ / h are arranged in two containers. Two silos with neutralizing agents 7 and each 60 m ³ storage volume are executed. The stock is enough for 1.3 tons per day for two weeks. The flocculant dosage is via screw conveyors. The air is introduced through special aerators 6 according to the airlift principle as mammoth pumps 6 , The neutralizing agent 7 is dosed dry in the rising air-water emulsion. By deflecting the water-lime-air mixture in the reaction tank 2 Intensively circulated several times to ensure the best possible solution of oxygen and neutralizing agent in the water. About the dosage of hydrated lime 7 a pH> 8.5 and the associated reaction rate are controlled. The reaction rate and the dosing of air are in turn coordinated so that the essential processes of iron oxidation and acid neutralization within the residence time in the reaction container 3 be completed.

Then the water gets into the next container 14 transferred with a total volume of 2 × 40 m ³ and a polymeric flocculant FHM added. For example, Synthofloc 8012 HL, which is an anionic polyacrylamide, in a specific dosage of 0.4 to 0.8 g / m ³ or 360 to 720 g / h or 8.6 to 17.3 kg per day is used as a flocculant , The flocculant FHM is dosed from a pre-prepared stock solution, which is delivered in transportable 0.8 m ³ containers. Or: The preparation of the flocculant auxiliary suspension and the dosing station are in a separate container next to the flocculation aid injection basin 12 accommodated. The admixing of the flocculant FHM is carried out with a vertically mounted stirrer 16 with adjustable rotational speed. After flocculant addition, the water is added to the second chamber of the container 14 , the flake-ripening basin 13 , convicted. The flocculation is optimized by a horizontally mounted drum paddle.

Finally, the water 5a in a third module 21 into a large sedimentation container 23 transferred with preferably lamellar separators with 160 m ² lamellar surfaces, which offer a favorable utilization ratio of 0.28 m ³ / m ² / h.

The number of sedimentation containers can optionally be increased according to the desired degree of separation. The sedimentation container 23 is for the purpose of transfer to a fourth module 31 with two mud pumps 32 equipped with 2.5 to 5.0 l / s pumping capacity. Four mud pumps 32 are for transfer to the fourth module 31 , that is to the pre-thickener 33 , intended.

The purified water is knocked off into the receiving water. This is done via the clear water drain line 26 , The thickened sludge is automatically dewatered and transported away in a further process step. The fourth module 31 includes in addition to the pre-thickener 33 or sludge thickener 33 a sludge dewatering unit 34 with a decanter and with a pump. For the transport of the thickened sludge is a sludge container 35 intended. From the sludge thickener 33 off is a clear water return 36 in the sedimentation container 23 intended.

Second exemplary embodiment: Design of a container-supported water treatment plant for 100 l / s well water

Due to the ongoing increase in groundwater re-emergence, groundwater containing highly iron-containing groundwater is leaving some of the flowing water sections in southern Brandenburg. Since the year 2007, an increasing iron load has been detected in the Spree. The aim is to reduce the pollution in the Spree by removing locally heavily polluted groundwater in the stream to the receiving water and its ironing in a water treatment plant.

In the second embodiment, iron-rich water is to be treated from two well bolts in the water treatment plant.

The feed water to be treated is characterized by the following values: Flow rate: 85 to 100 l / s Average pH value: 5.4 Mean iron (II) concentration: 100 mg / l Medium acidity: 3.3 mg / l.

It should be in the water treatment plant 360 m ³ / h iron-containing water to be cleaned. The objective of the temporary water treatment is a substantial reduction of iron loads. The total drainage concentration of iron is at most 10% of the feed concentration.

The 5 shows a modular water treatment plant for the de-ironing of oxygen-free groundwater, which is obtained via wells.

• • vier Stück Reaktionsbecken 2 mit Belüftung in Abrollcontainern 3 mit einem Volumen von jeweils 40 m³,
• • zwei Gebläsestationen 30 zum Betrieb der Belüfter 6 in den Reaktionsbecken 2 innerhalb der Container 3,
• • zwei Siloanlagen mit einem Nutzvolumen von jeweils 60 m³ zur Bevorratung des Neutralisationsmittels Kalkhydrat 7 als Flockungsmittel,
• • zwei Flockungsmitteldosierstationen in den Reaktionsbecken 2,
• • zwei Flockungsreifungscontainer 14,
• • sechs Sedimentationsbecken 22 mit Lamellenseparatoren 25 in Containern 23 des Volumens von 40 m³ mit jeweils zwei Schlammpumpen 32 mit 2,5 bis 5 l/s und einer Überleitung 28 zu einem Voreindicker 33,
• • ein Schlamm-Voreindicker 33,
• • ein Schlammrücklauf 37 vom Voreindicker 33 in die Flockungsreifungsbecken 13 zur Bildung größerer, besser absetzbarer Flocken,
• • ein Dekanter 34 für die Schlammentwässerung und
• • eine Ablaufleitung 26 von der Wasseraufbereitungsanlage in Richtung Vorfluter.

The essential parts of the plant for implementing the objective are in the 5 shown schematically:

• • four pieces reaction tanks 2 with ventilation in roll-off containers 3 each with a volume of 40 m ³ ,
• • two blower stations 30 to operate the aerators 6 in the reaction tank 2 inside the container 3 .
• • two silo plants with a useful volume of 60 m ³ each for storing the neutralizing agent hydrated lime 7 as a flocculant,
• • two flocculent dosing stations in the reaction tanks 2 .
• • two flocculation maturing containers 14 .
• • six sedimentation basins 22 with lamellar separators 25 in containers 23 the volume of 40 m ³ , each with two mud pumps 32 with 2.5 to 5 l / s and a transfer 28 to a pre-thickener 33 .
• • a sludge pre-thickener 33 .
• • a mud return 37 from the pre-thickener 33 into the flocculation tanks 13 to form larger, better settable flakes,
• • a decanter 34 for sludge dewatering and
• • a drain line 26 from the water treatment plant in the direction of receiving water.

Reaction tank 2:

The waters are after the removal and quantity measurement for iron removal in a reaction tank 2 initiated. In this reaction tank 2 is via screw conveyors from two silos of hydrated lime 7 about the special mammoth pumps 6 with aerator attachment 8th introduced into the reaction tank. At the same place, the mine water entry is accomplished. This ensures good mixing with simultaneous entry of oxygen and hydrated lime.

The addition of hydrated lime 7 is required to raise the pH to 8.5 to 9. This area is required to achieve complete iron oxidation in this water.

The amount of lime is controlled via an online pH measurement. The speed of the conveyor spiral is adjusted. This is done fully automatically via a stored algorithm depending on the pH value and setpoint specification.

At the same time air is introduced for the oxidation. This is done via five mammoth pumps 6 that stuck with the container 3 are connected. The necessary quantities of air are supplied via a blower station 30 generated. The blower station 30 is located on the side and connects the pumps via pipes and compressed air hoses. There are two fans per street 30 intended for air production. A fan 30 generates the necessary amount of air for the two reaction tanks. The circuit of the blower 30 always takes place alternately. The second fan is available as redundancy. The power consumption of a blower is 11 kW.

The reaction tank 2 is to be dimensioned according to the known state of the art, depending on the required reaction oxygen, for a residence and reaction time of 5-10 min.

This means that with an inflow of 360 m ³ / h and a residence time of 10 min, the pool must have a volume of 60 m ³ . Since the amount of air required for the reaction process at the example site is considerable (see calculation of oxygen input), a multi-lane expansion of the plant will be carried out with two parallel roll-off containers measuring 7.0 × 2.35 × 2.4 m, with a maximum usable volume of 39.5 m ³ and two additional reaction tanks set up one behind the other 2 each road, with a useful volume of 35 m ³ , in total 140 m ³ provided. The reaction time is limited to 26 minutes.

Calculation of the hydrated lime quantity:

Calculation of the lime was based on the above mentioned iron loads from the wells. The average pH of the rated water is pH 5.4. The amount of hydrated lime needed to raise the pH to> 8 is 370 g / m ³ (185 g / m ³ per road) for the design water. With a treatment volume of 360 m ³ / h (100 l / s) 1.6 t / d are required. Each treatment line requires approx. 0.8 tons per day of lime at a flow rate of 50 l / s. The loss of efficiency of hydrated lime (ŋ = 80%) has already been considered.

For the planned 60 m ³ useful volume and a bulk density of 0.45 t / m ^3, the maximum stocking for the location is about 17 days. The exact required Kalkdosierung via the frequency-controlled spiral conveyors. There is a pH probe in the drain area of the second reaction tank and provided in the feed duct. Thus, the dosage can be realized via a stored in the control matrix.

Interpretation of the ventilation for the entry of the specific oxygen demand of 46 mg / l:

For the oxygen calculation, the above-mentioned iron loads from the well bolts were used. During iron removal, iron (II) ions (Fe ² +) dissolved in water are first oxidized to trivalent ions. The oxidation takes place with oxygen (O ₂ ), which is introduced into the medium via the introduction of air. For rapid oxidation, the pH should be set to 8.5. Calculated, the following specific oxygen demand for the oxidation of Fe (II) is required:
Existing iron load: 118.5 mg / l: 55.85 mg / mmol = 2.12 mmol / l ≡ 2.12 mol Fe (II) / m ³ .

At the inlet flow rate of 360 m ³ / h and the average iron load of 118 g / m ³ are stoichiometrically 3.2 mol O ₂ / min (≡ 101.4 g O ₂ / min) required for oxidation. It is calculated with a stoichiometric factor for the reaction of 4 (4 moles iron Fe per mole of oxygen O ₂ oxidized).

Taking into account the Avogadro constant with respect to the molar volume of 22.4 l / mol, this results in 71.0 liters of O ₂ / min as the material flow to be introduced. This corresponds to 355.0 liters of air / min.

With an estimated efficiency of 6% for the aerators of 20%, the air volume to be injected is 106.5 m ³ / h. This amount of air is required to completely oxidize the Fe (II) contained in the raw water. This comes with the total of 20 pieces of mammoth pumps 6 in four containers 3 as shown in 5 safely reached.

The entry concentration of the used mammoth pumps 6 for oxygen is 6 g / m ³ for very warm water, as is typical for summer operation. This results in a necessary water flow through the mammoth pumps 6 of 16.90 m ³ / min = 1,014 m ³ / h. Each of the aerators 6 , circulates at least 1.0 m ³ / min, with two of the total of 18 aerosols intended for lime entry. The air volume of around 107 m ³ / h is sufficient to get the water through the aerators 6 to move. A mammoth pump 6 promotes 20 m ^{3 of} air per hour at a minimal rate.

Flocculant injection and ripening container 14 :

The task of the water treatment plant is to remove precipitable or suspended foreign matter from the water. This happens here for the iron constituents by separation via sedimentation in the sedimentation basin.

This mechanical separation stage is preceded by a chemical process by which the foreign substances contained in the water are first converted into a mechanically separable form. These include:
the neutralization and oxidation in the reaction tank 2 and
the flocculation of the already colloidally suspended substances from pulps using flocculants and flocculants.

• • eine Entstabilisierung des Kolloids, durch die eine Zusammenlagerung einzelner kolloidaler Teilchen zu größeren Einheiten stattfinden kann (Koagulation) und
• • eine als Flockung bezeichnete Zusammenballung sehr vieler dieser Einheiten zu größeren, spezifisch schweren und damit mechanisch abtrennbaren Flocken.

The flocculation of a colloid requires two partial reactions, which in practice more or less merge into each other:

• • a destabilization of the colloid, through which an aggregation of individual colloidal particles can take place into larger units (coagulation) and
• • a flocculation of a large number of these units into larger, specifically heavy and thus mechanically separable flakes.

For optimum flocculation, the amount of 0.4 g / m ³ or 144 g / h of FHM should be metered into the feed water. In order to be able to set the optimum amount during the run-in process, the dosing flow must be variable. For this reason, a dosing capacity of 0.3-0.6 g / m ³ or 108-216 g / h at a flow rate of 360 m ³ / h is provided on the basis of preliminary tests on a pilot plant scale. The polymer is prepared in a piecing station to a 0.1% solution. For this purpose, approx. 2 m ³ drinking water must be supplied. The station is designed as a pendulum system for continuous operation. Depending on the road (50 l / s), it is therefore necessary to meter in polymer solution between 54 and 108 l / h (0.3-0.6 g / m ³ ) in the case of a 0.1% strength solution. The dosage is done separately for each street via an eccentric screw pump. With an optimum polymer use of 0.4 g / m ³ 144 l / h (0.1% solution) are to be metered per road. The start-up and dosing station is housed as a compact station in a 10-foot sea container (3.0 × 2.44 × 2.59 m). The container is delivered to the construction site ready-equipped with the system components, the switchgear, light, heating and piping. The on-site electrical supply and the drinking water connection with a nominal diameter of DN 25 are to be carried out on site. The attachment station is a shuttle with 500 l / h start-up capacity. This enables the batchwise approach for continuous operation. It is to set up the solution, a reservoir for 60 liters of granules on the plant available. The container is filled manually by the operating personnel. At a consumption of 0.4 g / m ^3, a filling is sufficient for about 21 days in a 24 h operation. At the maximum rate of 0.6 g / m ³ , it is 14 days. The use of successively connected, slow-running vertical and horizontal agitators for the addition of flocculant and flocculation in a multi-chamber arrangement can save dosing. For the introduction of the flocculant FHM is an injection chamber 12 for the flocculation aid (FHM chamber) with paddle mechanism 16 and the internal dimensions of 2,500 × 6,500 mm necessary. In the downstream ripening room 13 is a drum paddle (type: L8 / D2.5) installed per expansion stage, the flake-water mixture gently to the sedimentation basin 22 emotional.

Sedimentationsbecken 22 :

The transfer takes place via a pipeline in pairs to the flocculation containers 14 standing sedimentation container 23 , In the conventional water treatment plants, which are designed as standard, sedimentation is usually carried out in large round or rectangular tanks with a residence time of at least two hours and corresponding sludge removal facilities. In order to be able to carry out sedimentation in tanks as small as rolling containers, oblique clearers or so-called plate or lamellar clarifiers (cf. 3 ) used. The prerequisite is a minimum flake size of 50 micrometers to be achieved by the described upstream devices. The sedimentation basin 22 are in 40 m ³ roll-off containers 23 accommodated. These are equipped with honeycomb packs with 60 ° inclination on holding structures made of stainless steel. The lamella packages have an area of 250 m ² per package. The Total capacity for the example site amounts to six sedimentation containers 23 each with 160 m ² lamellar surfaces, three each for 50 l / s. Here the utilization ratio amounts to 360 m ³ per 960 m ² and thus to 0.375 m ³ / m ² h. The utilization ratio should not exceed 0.6 to 0.8 m ³ / m ² h. Above the slats is a clear water drainage channel with tooth sills 27 made of stainless steel. Thus, there is sufficient area to achieve the particle deposition in sufficient quantity. The aim is 95% iron removal. At around 100 mg / l in the inflow, this is around 5 mg / l in the effluent.

The sludge collecting space below the slats is equipped with side slits and two sludge extraction pipes with a nominal diameter of DN 150 with slotted holes ( 3 ). The resulting sludge we use mud pumps at the rear of the container 23 aspirated. From the downstream sludge collection room is the pre-thickener 33 filled. The extracted Eisenhydroxidschlamm is about the Schlammabsaugrohrsystem into the pump sump sedimentation container 23 promoted. The resulting Eisenhydroxidschlamm is a container with Krählwerk the pre-thickener 33 , forwarded and pre-thickened there. From the pre-thickener 33 be over the mud return 37 about 15% of the feed sludge back to the flocculation tank 12 returned to improve floc size and flocculation.

The purified water is through the clear water drain line 26 derived. The thickened sludge is automatically dehydrated in a further process step and preferably transported away for reuse. For drainage is a sludge dewatering unit 34 with a decanter 34 and a pump provided. For the transport of the thickened sludge is a sludge container 35 intended. From the sludge thickener 33 off is also a clear water return 36 in the sedimentation container 23 intended.

LIST OF REFERENCE NUMBERS

1

first module 1

2

 reaction pool

3

 Container of the first module "Reaction tank"

4

 Inlet, inlet pipe

5

 Inlet water, (iron-rich) water

5a

Water in the containers 3 . 14 and 23 as well as their connecting lines

5b

Water level in the containers 3 . 14 and 23 , Liquid level

6

 Aerator, mammoth pump, pipe, aerator

6a

 Belüfterfuß

6b

 Belüfterausgang

7

 Neutralizing agent, flocculant, hydrated lime

8th

 Aerator attachment, attachment

8a

 tower entrance

9

 funnel

10

Expiration (of the first module 1 )

11

 second module

12

 Injection basin, flocculation aid adding basin, injection chamber

13

 Flockungsreifebecken

14

 Container of the second module "flocculation"

15

Supply line for the injection basin 12

16

 vertical paddle work

16a

vertical axis of paddling 16

17

 Transfer port

18

 vertical deflection wall

19

 horizontal paddling work

19a

horizontal axis of paddling 19

20

 Transition to sedimentation

21

 third module

22

 Sedimentationsbecken

23

 Container of the third module "sedimentation", sedimentation container

24

Inflow into the sedimentation basin 22

25

 Lamella separators, plate separators

26

 Clear water drain lines, drain line

27

 Clear water extraction device, clear water drainage channel, clear water drainage channel with toothed thresholds

28

 Pipe systems (for sludge water removal), sludge removal device, transfer

29

 Removal structure, removal shaft

30

 Blower station, blower

31

 fourth module "sludge treatment"

32

 slurry pump

33

 Pre-thickener, sludge thickener

34

 Sludge dewatering unit, decanter

35

 sludge container

36

 Clear water recirculation

37

 Sludge recirculation

FHM

 flocculants

MID

 Magnetic-inductive flowmeter

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited patent literature

• DE 29502118 U1 [0007]
• AU 002011274292 A1 [0007]
• DE 19834727 A1 [0009]

Claims (7)

Modular system for the flexible de-ironing of water, comprising - a first module ( 1 ) with one or more parallel or series containers ( 3 ), containing in each case at least one reaction tank ( 2 ) with several aerators ( 6 ), whose principle of operation is based on the principle of a mammoth pump ( 6 ) or an ejector, of which at least one aerator ( 6 ) with a ventilator attachment ( 8th ) for introducing a solid into the reaction tank ( 2 ), - a second module ( 11 ) with one or more parallel or series containers ( 14 ) containing in each case at least one injection basin ( 12 ) for the injection of a flocculant and at least one flocculation basin ( 13 ) for iron hydroxide flakes to be deposited, - a third module ( 21 ) with one or more parallel or series containers ( 23 ) containing in each case at least one sedimentation basin ( 22 ) for the sedimentation of iron hydroxide flakes and a clear water withdrawal device ( 27 ). Modular system according to claim 1, further comprising a fourth module ( 31 ) for the treatment of sedimentation basins ( 22 ) of the third module ( 21 ) via a sludge removal device ( 28 ), wherein the sludge treatment takes the form of a sludge thickening in a sludge thickener ( 33 ) and / or sludge dewatering in a decanter ( 34 ). Modular system according to claim 1 or 2, characterized in that in the second module, the injection basin is provided as a first basin for injection of a flocculation aid, preferably a polymer, wherein the injection basin for the interference of the injected flocculation aid has a Vertikalpaddelwerk. Modular system according to one of claims 1 to 3, characterized in that in the second module a the injection basin subsequent ripening is provided for the growth of the iron flakes to be deposited, in which a horizontal paddling for the provision of the necessary kinetic energy for flocculation and for non-destructive lifting of the grown flakes is arranged in a transfer line for sedimentation. Modular system according to one of claims 1 to 4, characterized in that in the third module in the sedimentation basin for efficient deposition lamellar separators (plate) are arranged in an inclined position. A method of flexible deferrisation of water in a modular system according to any one of claims 1 to 5, in which a) the iron-rich water for deferrisation in the first module ( 1 ) in a reaction tank ( 2 ) via an inlet ( 4 ) and in the reaction tank ( 2 ) at least one neutralizing agent, preferably hydrated lime ( 7 ), via at least one aerator ( 6 ), whose principle of operation is based on the principle of a mammoth pump ( 6 ) or an ejector and which is equipped with a ventilator attachment ( 8th ) for introducing a solid into the reaction tank ( 2 ), while at the same time oxygen is introduced via this and optionally other aerators ( 6 ) into the water ( 5a ) of the reaction tank ( 2 c) a flocculation of already present colloidally suspended iron hydroxide and other solids in the water treated by process step b) in the second module ( 11 ) by injection of flocculants (FHM) in an injection basin ( 12 ) and then ripening of the iron hydroxide flakes to be deposited in a flocculation basin ( 13 ) and d) the sedimentation of the iron flakes takes place in one or more parallel operated containers in a third module and the supernatant clear water through a clear water withdrawal device ( 27 ) a clear water drain line ( 26 ) is supplied. A method according to claim 6, characterized in that the neutralizing agent in suspension via an aerator ( 6b ) with the aerator attachment ( 8th ) associated aerators ( 6 ) in the water of the reaction tank ( 2 ).

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