DE10129307A1 - Filtration unit for removing pollutants from fluids, especially water, comprises agglomerates of finely divided iron oxide and oxyhydroxide - Google Patents

Abstract

Filtration unit for removing pollutants from fluids contains agglomerates of finely divided iron oxide and oxyhydroxide with a BET surface area of 50-500 m<2>/g. Filtration unit for removing pollutants from fluids, comprising a cartridge housing (4) consisting of a container with a central inlet tube (6), top and bottom flat filter layers (3, 10), a lid with a fluid inlet (1) and outlet (12) and a base (9), contains a bed of agglomerates of finely divided iron oxide and oxyhydroxide with a BET surface area of 50-500 m<2>/g, where the agglomerates optionally contain iron oxide pigments with lower BET surface areas provided that the content of these is at most such that the resistance of the bed to the forces exerted on it by the flowing medium is high enough for the stressing of the bed by the flowing medium not to result in unwanted abrasion of the bed material when the fluid to be purified passes sequentially through the inlet connector (1), inlet tube (6), sieve basket (7), optional filter material (8) in the bottom space (9), the lower frit plate (10), the adsorber material (5) in the contact chamber (4), the upper frit plate (3), the filter material (2) in the lid and the outlet tube (12). Independent claims are also included for the following: (1) a process for producing agglomerates of finely divided iron oxide and oxyhydroxide in lump form, comprising: (a) preparing an aqueous suspension of finely divided iron oxide and oxyhydroxide with a BET surface area of 50-500 m<2>/g; and (b) removing water and dissolved components either by: (i) removing the water, redispersing the residue in water, filtering the suspension, washing the residue, and either dewatering and comminuting the filter cake or partially dewatering the filter cake and shaping and drying the resulting paste; or (ii) filtering the suspension, washing the residue to obtain a filter cake in the form of a low-salt paste, either dewatering and comminuting the filter cake or partially dewatering the filter cake and shaping and drying the resulting paste, and optionally grinding or granulating the product; (2) a process for producing an adsorbent/reactant, comprising: (a) mixing aluminum, magnesium and titanium oxides or (oxy)hydroxides or their aging or dehydration products into an aqueous suspension of iron oxide and oxyhydroxide, including Fe(OH)2; and (b) either drying the suspension to form a solid and comminuting the solid or mechanically shaping the optionally predried suspension in semisolid form and drying the product to form a solid.

Description

The invention relates to a fluid through which a liquid to be treated can flow Adsorption container, in particular a filter adsorption container, filled with granulated or powdered, solid, water-insoluble adsorption media, ins special iron (oxi) hydroxide, for removing arsenic or heavy metals Drinking water is used. The device can e.g. B. in the household to the sanitary and drinking water supply.

The invention further relates to a process for the preparation of iron (oxi) hydrox id adsorber for filling in the filtration units according to the invention.

National Academy of Science studies in 1999 found that arsenic in drinking water Bladder, lung and skin cancer.

The problem is often faced, especially in regions where wells, Tap or general drinking water with arsenic or other heavy metals is contaminated, no suitable drinking water treatment plant nearby or none have a suitable unit at hand that continuously removes the pollutants would.

Filter cartridges, for cleaning liquids, preferably contaminated ones Water, which can also contain an adsorption medium, is available in different Executions known.

For the separation of solids from water z. B. membrane filter cartridges in suitable housings in use.

Cartridges and devices are from the company Brita Wasser-Filter-Systeme GmbH gene for the preparation of liquids known (DE-A 199 05 601; DE-A 199 15 829; DE-A 198 14 008, DE-A 196 15 102, DE-A 43 04 536, US-A  6,099,728). These devices are well suited for whole or partial desalination of drinking water in household cans immediately before using the Drinking water.

From US-A 4,064,876 a filtration unit designed as a filter cartridge is knows that between a polyester urethane foam layer and a glass fiber layer has a bed of activated carbon particles.

DE-A 198 16 871 (Sartorius) describes a filtration unit for removing harmful substances described substances from fluids.

In RU-A 2 027 676 there is a cartridge filter with sorbent for drinking water free described with connection to the tap in the apartment.

In HU-A 00 209 500 is a filter cartridge for the removal of radioactive mate rial and heavy metals from water described with a mixture of ions exchange material, activated carbon, filter sand, zeolites, aluminum oxide and red is filled with mud.

Most of these are adsorber cartridges with activated carbon or with ion exchangers filled with resins. However, activated carbon has the disadvantage that arsenic and heavy metal salts, as they occur in aqueous systems, because of the low adsorption Capacity of the activated carbon can not be removed to a sufficient extent, which is affects the service life of the cartridges.

Ion exchange resins have the disadvantage that they are very ions from aqueous solution bind non-selectively and there are often competitive reactions in adsorption. Another disadvantage of ion exchangers is the strong dependence of the adsorp ion exchange capacity of the pH of the water, so that large men Chemicals are necessary to adjust the pH of the water, which is the case with Use of the adsorber cartridge in the household is not practical.  

Contact and adsorber granules, including those based on iron oxides and / or Iron oxyhydroxides have already been described. They are mostly in continuous processes, where they are usually in tower or column-like apparatus are located by the medium to be treated are poured, and find on the outer and inner surface of the granules chemical or physical reaction or adsorption processes instead. To the Powdery materials cannot be used for this purpose because they are compress in the direction of flow of the medium and thereby the flow resistance up to increase to block the apparatus. An apparatus is cleaned by backwashing nig (see below), large amounts of the powder are discharged, lost or lead to an intolerable pollution of the wastewater.

However, the flowing media also exert forces on the granules, which lead to the ab rasion and / or movement up to violent agitation of the granules can. This causes the granules to collide, and as a result, arises unwanted abrasion. This leads to loss of contact or adsorber material and contamination of the medium to be treated.

In gas cleaning, the agent is used in adsorbers for binding undesirable components such as hydrogen sulfide, mercaptans and hydrocyanic acid, as well as other phosphorus, arsenic, antimony, sulfur, selenium, tellurium, and cyano and heavy metal compounds in exhaust gases. It is also possible to adsorb gases such as HF, HCl, H ₂ S, SO _x , NO _x .

A filter cartridge for drying gases is e.g. B. described in US-A 5,110,330 ben.

It is also possible to remove phosphorus, arsenic, antimony, selenium, tellurium, as well as cyano and heavy metal compounds from waste oils and other contact mined organic solvents.  

Contact and adsorber granules based on iron oxides and / or iron oxihy Droxides are also used to catalyze chemical reactions in the gas phase or in the liquid phase used.

Various methods are known for using adsorbents to remove the trace and pollutants from aqueous systems.

DE-A 38 00 873 describes an ad for removing pollutants from water sorbent based on porous materials such as hydrophobic chalk with fine to medium grain.

DE-A 37 03 169 describes a process for producing a granulated filter disclosed for the treatment of natural water. The adsorbent is by Gra nulation of an aqueous suspension of kaolin with the addition of powder Dolomite produced in a fluidized bed. Then the granules at Fired 900 to 950 ° C.

DE-A 40 34 417 discloses a process for the production and use of highly reactive reagents for exhaust gas and waste water purification. Described here are mixtures of Ca (OH) ₂ with additions of clays, stone flour, fly dust and fly ash, which are made porous and have a surface area of approx. 200 m ² / g.

The procedures mentioned and the contacts used for this have in common same disadvantage that the respective for the selective adsorption of ingredients component responsible for cleaning media, i.e. the actual adsorbent, with large amounts of aggregates must be added to a shape to admit to granules. This significantly lowers the bandage capacity for the water pollutants to be removed. In addition, the later Auf Processing or recycling of the material is problematic because it is used as a binder foreign substances used must first be separated again.  

DE-A 42 14 487 describes a method and a reactor for removing Impurities from water described. A funnel-shaped reactor in which as Sorbent for water contamination finely divided iron hydroxide in flaky form flow is horizontal. The disadvantage of this method is that Use of the flaky iron hydroxide, which is due to its low density difference between water and iron hydroxide leads to such a reactor can only be operated at very low flow speeds and There is a risk that the sorbent, possibly already loaded with pollutants, is discharged from the reactor together with the water.

JP-A 55 132 633 describes granulated red mud as a by-product of aluminum production as an adsorbent for arsenic. This is composed of Fe ₂ O ₃ , Al ₂ O ₃ and SiO ₂ . The stability of the granules and the granulation process are not reported here. Another disadvantage of this adsorbent is the lack of consistency in the composition of the product, the uncertain availability and the possible aluminum contamination of the drinking water. Since aluminum is suspected of favoring the development of Alzheimer's disease, contamination with it must be avoided in particular.

DE-A 198 26 186 describes a process for producing an iron hydroxide holding adsorbent described. An aqueous polymer dispersion is in Iron hydroxide mixed in water-dispersible form. This mixture will then either dried to a solid state and the solid mass material then mechanically crushed into the desired shape and / or size or the mixture is optionally pre-dried after shaping subjected and then finally dried to obtain a solid state. This gives a material in which the iron hydroxide is firmly in the polymer is embedded and that has a high binding capacity for the usually in wastewater or contain exhaust gases.  

The disadvantage of this process is the use of organic binders the water to be treated by washing and / or abrasion of organics additional burden. In addition, there is resistance to prolonged use of the adsorber not guaranteed. Bacteria and other microorganisms can or ganic binder also serve as a nutrient medium so that the risk of loading settlement of contact with microorganisms and contamination of the medium through them.

Basically, the presence of is necessary for the production of the adsorbents non-native auxiliaries in the processing, recycling or expansion re-use of used adsorbents is disadvantageous because the re-use is pure Substances are less problematic than is the case with mixtures of substances. So are for example polymeric binders in the further use of adsorber materials materials based on iron oxide as pigments for coloring concrete are disadvantageous because these binders hinder the dispersion of the pigment in the liquid concrete.

DE-A 43 20 003 describes a process for removing dissolved arsenic Groundwater is described using colloidal or granulated iron hydroxide. For the use of fine, suspended iron (III) hydroxide products is here Recommended to put the iron hydroxide suspension in grease bed filter with granular mate rial or other carriers are filled with high external or internal porosity bring to. This method also has the disadvantage that, based on the Adsorbent "substrate + iron hydroxide", only low specific loading capacity ten can be reached. In addition, there is only a weak bond between the substrate and iron hydroxide, so that subsequent treatment with arsenic Water there is a risk of iron hydroxide or iron arsenate being discharged. In this publication continues to use granulated iron hydroxide as Adsorber material for a fixed bed reactor called. The production of the granulated Iron hydroxide takes place via freeze conditioning (freeze drying) iron hydroxide obtained by neutralizing acidic iron (III) salt solutions at temperatures below minus 5 ° C. This manufacturing process is high  energy-intensive and leads to heavily salt-contaminated wastewater. In addition, as Result of this manufacturing process is only very small granules with less maintain mechanical stability. This leads to use in a fixed bed Actuator that the grain spectrum by mechanical abrasion of the particles significantly decreased in the course of operation, which in turn has the consequence that fine disperse particles of loaded or unloaded adsorbent from the Re actuator. Another disadvantage of these granules is that the Ad sorptive capacity against arsenic compounds is significantly reduced if the granules, e.g. B. due to longer dry periods, lose water.

From US-A-5,948,726 Adsober / Binder systems have become known by using a mixture of (a) a crosslinkable binder from colloi dalen metal or metalloid oxides, (b) oxidic adsorbents such as metal oxides and (c) withdrawing a sufficient amount of water from an acid so that components (a) and (b) crosslink to form an adsorbent / binder system Zen. According to the exemplary embodiments, colloidal alumina or Alumina used.

A disadvantage of these compositions is that which is necessary for their production Use of acid (column 9, line 4) and the fact that it is not pure, son heterogeneous substances, which are used for the production, regeneration, ent supply or final storage of such adsorbers, for. B. on a landfill, undesirable is. Adsorbers are also included in the scope of disclosure of this document Adsorption of arsenic are suitable; however, concrete examples are not provided provides. Alumina is known for its adsorption power for arsenic clearly inferior to the iron oxides.

Continuously operated adsorbers are preferably used for water treatment sets that are often operated in groups arranged in parallel. For example To rid drinking water of organic contaminants, such ad sorber charged with activated carbon. Then at peak consumption times  existing adsorber operated in parallel so as not to exceed the flow rate to allow the design-related maximum to increase. During times low individual water adsorbers are taken out of operation and can be maintained, for example, while the adsorber material is exposed to special loads, as detailed below becomes.

The use of granules, which can be obtained by compacting z. B. powder can produce iron oxide by applying high linear forces already considered. Such granules have already been described for liquid concrete to dye homogeneously. The application of high linear forces when compacting is in high energy and costly and the stability of the compact is long-term use in adsorbers is insufficient. Therefore, such do not come for the Use in e.g. B. adsorbers, especially continuously operated, at Reini consideration of water. Especially when maintaining or cleaning the ad sorber systems by backwashing (see below) lose such granules through the associated agitation of the same large amounts of substance. The backwash Wastewater is badly clouded by abrasion. This is not for several reasons acceptable: First of all, adsorber material is lost, which after a long service life, loaded with impurities and therefore toxicologically is conceivable. Then the wastewater flow is loaded with the abrasion, the sediment Ren and thus leads to the impairment of the piping systems and ultimately the Sewage treatment plant physically and toxicologically undesirable to just a few To give reasons.

The present invention was also based on the object of a filtration unit for removing arsenic and heavy metals from drinking, custom, mineral, gar pond, agricultural, holy and medicinal water using iron oxyhydroxide or provide iron oxide particles as contact or adsorption / reaction agents len, due to the adsorber performance of the filling medium, a high removal of the dissolved Ensure most pollutants, which at the same time the mechanical and hydraulic  withstands stresses in the adsorber housings and in addition to Si safety due to the filtration performance of built-in filters Contamination or abraded, possibly contaminated with Ad prevent sorber parts.

The contacts or adsorbents / reactants according to the invention, their Provision, their use and apparatus loaded with them solve this complex task.

The object is achieved by a filtration unit which consists of a housing made of plastic, wood, glass, ceramic, metal or a composite material, which is provided with inlet and outlet openings. Insurance forms Exemplary simple exporting shown in the figures Fig. 1a and Fig. 1b. These housings are described in detail in DE-A 198 16 871. The inlet and outlet openings are separated from the actual housing space, which contains a bed of the iron oxyhydroxide adsorption medium, by flat filter systems covering them. The fluid to be treated thus successively passes through the first flat filter layer, the adsorber particles, the second flat filter layer and the outlet opening. The housing space can be completely or partially filled with the adsorber particles. The housing space is preferably conical or pyramidal, but can also be cylindrical, kugelför shaped, cuboid or serpentine. By tapering the housing space (see figure Fig. 1b) z. B. who achieved that the filtration can be operated in any position and no by pass between the bed of adsorber particles can be formed, which the fluid to be filtered can pass unhindered without adsorption. By filling the housing space with a bed of the adsorber particles, which takes up between 97 and 99% of the housing volume, a high flow rate of the fluid to be cleaned is ensured, since the stability of the adsorber granules counteracts the inflowing liquid with little resistance.

In preferred embodiments of the invention, the housing space is in the tapered sections formed as a truncated cone or as a truncated pyramid.

For the flat filter layers z. B. in DE-A 198 16 871 different materials shown.

An improved embodiment of an adsorber is shown in Figure Fig. 2a and Fig. 2b. They each show the household filter module in a longitudinal section.

The adsorber housing ( 4 ) with the Eisenoxihxdroxid adsorber material ( 5 ) with top ( 3 ) and bottom ( 10 ) arranged filter plates and centrally arranged inlet pipe ( 6 ) can be combined as a unit by screwing with the lid ( 13 ) at the upper end and a screw connection with the floor attachment ( 9 ) at the lower end by loosening the screw connections. Once the cartridge is loaded, you can insert a new one and clean the base and cover plate. At the upper end, the inlet pipe ( 6 ) is firmly connected to the inlet connector ( 2 ) via a suitable sealing ring during use. The inlet tube can be removed from the cartridge housing and inserted into a new, fresh cartridge housing. As a result, the incoming liquid flows directly to a sieve basket ( 7 ), which pre-filters suspended suspended matter, algae and the like and retains them at the entrance to the actual adsorber cartridge, so that the adsorber material does not bake or stick. The sieve ( 7 ) is used for even distribution of the incoming liquid flow into the floor space, is therefore preferably conical, ie frustoconical and completely surrounds the inlet pipe and is fi xed with both the sem and with the surrounding filter plate ( 10 ) via loose sealing rings. The fabric of the sieve can be made from common fine-mesh filter materials, e.g. B. consist of plastic, natural material or metal.

The screwed-on bottom part ( 9 ) can additionally contain a suitable filter material or filter flow ( 8 ), which can be selected depending on the type and amount of the suspended matter to be expected. If there are large amounts of solid foreign substances, the sieve ( 7 ) and the filter flow ( 8 ) can be easily removed and cleaned by unscrewing the bottom part. The filter plate ( 10 ), which can be made of fine-pored ceramic, separates the bottom space ( 9 ) from the contact space with the iron oxyhydroxide granules ( 5 ), so that no adsorber material gets into the bottom space and no pre-filtered material gets into the contact space. By passing the water to be cleaned from the contact area with the iron oxyhydroxide adsorber from bottom to top, the pollutants to be removed are removed by physical and / or chemisorption on the adsorber material. An additional filter plate at the upper end of the cartridge housing ensures that no adsorber material gets into the outlet ( 12 ). Due to increased water pressure or a long service life of the adsorber tank, fine particles can rub off from the adsorber material and pass through the filter plate ( 3 ). In order to avoid that this (loaded with pollutants) fine part gets into the outlet, filter material or filter flow ( 11 ) is embedded inside the cover ( 13 ), which retains the fine part.

The filter layers ( 3 ) and ( 10 ) also serve to distribute the fluid evenly over the adsorber space ( 5 ) or to collect it again after exiting from it. The clean water, cleaned of foreign and harmful substances, leaves the adsorber tank via the outlet connection ( 12 ).

The cover ( 13 ) can additionally have a valve in order to let the gases which are conveyed during the first operation during operation (e.g. air contained in the cartridge housing) escape.

Depending on the application, it may be advantageous to operate the adsorber tank just described in reverse order ( Fig. 2b). This means that the water to be cleaned now flows from the inlet connection ( 1 ) directly to the pre-filter ( 11 ) through which suspended matter and foreign bodies are retained, then passes through the filter plate ( 3 ) and enters the contact space, where the adsorption of the dissolved pollutants on the adsorber excess material occurs, passes through the cartridge base plate ( 10 ) into the floor space ( 9 ), where filter material ( 8 ) may be embedded in order to retain abraded adsorber material, the strainer basket ( 7 ) providing additional filtration services so that the cleaned water over the outlet pipe ( 6 ) and the outlet connection leave the adsorber tank via the opening ( 1 ).

Fig. 4 shows a simpler embodiment, which however works on the same principle as described above . It shows the adsorber tank which contains the adsorber granules according to the invention and in which the adsorber cartridge forms a unit.

In principle, other embodiments and designs are of course possible, which the structures described are similar and ar according to the ways described work, d. H. an inlet and outlet for water and iron oxide and / or Contain iron (oxi) hydroxide as adsorber media.

Figure 5 shows a filter bag which, filled with adsorber granules, can be fed into a water to be cleaned in order to remove the pollutants contained therein by adsorption.

Filter bags and extraction sleeves are known e.g. B. in various forms and from guides for the preparation of hot infusion beverages, especially tea. DE-A 83 94 05 describes e.g. B. such a folding bag, such as for the preparation of tea and the like is used. Through a special folding technique, through which a double chamber system is an intensive mixing of the eluent with the guaranteed substance to be extracted.

Conversely, iron oxides or iron (oxi) hydroxides in powdered, fine or coarse granulated form can also be embedded in semi-permeable bags or bags with a filter effect (such as the folding bag described above), and these packs can be fed to the water to be cleaned to thereby remove the pollutants from the water by adsorption on the adsorber material after a certain contact time (see Figure Fig. 5). On the one hand, the iron oxides and / or iron (oxi) hydroxides withstand the mechanical and hydraulic stresses in the filter bag and, on the other hand, the filter performance of the filter membrane prevents any fine part of the adsorption that may be caused by abrasion from entering the water to be cleaned.

The various embodiments of the present invention have in common sam that iron hydroxide or iron oxyhydroxide in fine, coarse or powdered form embedded in housings with filter effect and the one to be cleaned Allows liquid to flow through the filter housing or the filter pack supplies cleaning liquid and thus guarantees adsorption of the pollutants guaranteed.

To produce the granules according to the invention, an aqueous Sus Pension of finely divided iron oxyhydroxides and / or iron oxides according to the state of the Technology manufactured. The water and the stock dissolved in it can then be extracted from this parts are removed in two different ways:  

Method 1

For applications in which the mechanical strength of the Granules / contacts are made, you first remove only the water, e.g. B. by evaporation. A residue is obtained, which is next to the finely divided iron oxide and / or hydroxide also contains the entire salt load. This backlog will redispersed in water after drying, which requires only relatively little shear force must be turned. This suspension is then filtered and the back stand is washed essentially salt-free. The filter cake that one as a back is a solid to semi-solid paste, which usually has a water content has between 10 and 90 wt .-%.

This can then be completely or partially dewatered, and the so obtained Material can then be shredded into the desired shape and / or size the. Alternatively, the paste or filter cake, if necessary after a pre drying to achieve a sufficiently solid state, a shape and then (further) drying to achieve a stuffy condition be subjected. The later application of the granulate determines the preferred one Procedure for its manufacture and is for the expert on the particular Application area can be determined by simple preliminary orientation tests. Either the immediately dried filter cake and the dried moldings can NEN can then be used as a contact or adsorber.

Method 2

For applications where higher demands are placed on the mechanical strength of the Granules / contacts are made, the suspension is filtered and the residue washed essentially salt-free. The filter cake that you get as a residue is a solid to semi-solid paste. This can then be entirely or partially be watered, and the material thus obtained can then be in the desired Shape and / or size are crushed. Alternatively, the paste or filter cake, if necessary after pre-drying to obtain one After a solid state, a shaping and subsequent (further) drying  undergo a lumpy condition. The later application The granulate determines the preferred procedure for its production and is for the specialist in the respective field of application by simple ori final preliminary tests can be determined. Both the immediately dried filter ku Chen and the dried moldings can then be used as a contact or adsorber be used.

The products obtained according to method 1 are mechanically less stable, however, the filtration is easier and faster to do. They can also do that isolated fine-particle pigments very easily in z. B. incorporated paints and polymers be used, because you need considerably less shear force than it does for the Einar processing of the fine-particle pigments obtained according to Method 2 is required.

The finely divided iron oxide and / or iron oxyhydroxide used has a particle size of up to 500 nm, preferably up to 100 nm, particularly preferably 4 to 50 nm, and a BET surface area of 50 to 500 m ² / g, preferably from 80 to 200 m ² / g.

The primary particle size was determined by scanning electron microscopy, e.g. B. determined at a magnification of 60,000: 1 by measuring (device: XL30 ESEM FEG, Philips). Are the primary particles acicular, such as. B. in the phase of α-FeOOH, the needle width can be given as a measure of the particle size. With nanoparticulate α-FeOOH particles, needle widths of up to 100 nm are observed, but mainly between 4 and 50 nm. Α-FeOOH primary particles usually have a length: width ratio of 5: 1 to 50: 1, typically from 5: 1 to 20: 1. However, the doping or special reaction procedure hoist the needle shapes to vary in their length: width ratio. Are the primary particles isometric, such as B. in the phases α-Fe ₂ O ₃ , γ-Fe ₂ O ₃ , Fe ₃ O ₄ , the particle diameter may well be less than 20 nm.

By mixing nanoparticulate iron oxides or iron (oxi) hydroxides with pigments and / or Fe (OH) ₃ you can see on the scanning electron micrographs the presence of the given pigment or germ particles in their known particle morphology, which is due to the nanoparticles Seed particles or the amorphous Fe (OH) ₃ polymer are held together or glued together.

Products obtainable by methods 1) or 2) can then be used as examples be crushed further by grinding or grinding. Because the products the first time they come into contact with water, for example the first time they fill a fresh one If the adsorber apparatus is charged with water, but it is shredded autogenously, this is done in generally not required.

As another method of producing granules, the granulation has a half moist paste proven. Here you form pellets or strands from a semi-solid Paste e.g. B. Using a simple perforated plate, a roller press or an extru and either dries them immediately or brings these extrudates using a Spheronizers also in a spherical or granular form. The still wet balls Chen or granules can subsequently to any moisture content be dried. So that the granules do not cake, it is recommended a residual moisture content of <50%. Such a spherical shape can be used in Fixed bed adsorbers because of the better bed in the adsorber container be advantageous compared to crushed granules or pellets in strand form.

Generally it is possible to improve the filtration behavior of the suspensions to apply customary filtration-improving measures such as z. B. in solid Liquid Filtration and Separation Technology, A. Rushton, A. S., Ward R. G., Holdich, 2nd edition 2000, Wiley-VCH, Weinheim and manual of the industrial solid / liquid Filtration, H. Gasper, D. Öchsle, E. Pongratz, 2nd ed. 2000, Wiley-VCH Weinheim are described. For example, flocculants can be added to the suspensions be set.  

In addition to or instead of the iron oxyhydroxides, iron carbonates can also be used become.

The products according to the invention can be dried in air and / or in Va vacuum, and / or in the drying cabinet and / or on belt dryers or by spray drying, preferably at temperatures from -25 to 250 ° C, particularly preferably at 60 to 120 ° C, are subjected.

The products according to the invention preferably have a residual water content of less than 20% by weight.

It was found that the pieces or granules thus obtained had a high binding have capacity for pollutants contained in water, liquids or gases and they also have a sufficiently high stability against flowing media with regard to mechanical or hydraulic stress.

In particular, it is surprising that finely divided iron oxyhydroxides or iron oxides with high specific surfaces when drying in very hard agglomerates which have high mechanical abrasion resistance without the addition of binders and high hydraulic stability against contact with flowing through Have water, and a high binding capacity for those contained in the water have harmful and trace substances.

For the use of finely divided iron oxyhydroxides according to the invention, z. B. transparent iron oxyhydroxide pigments with specific surfaces of more than 80 m ² . However, it is also possible to use correspondingly finely divided iron oxide pigments, preferably hematites, magnetites or maghemites.

The production of yellow, finely divided iron oxyhydroxide pigments (e.g. goethite) in the acidic or alkaline pH range, so-called acidic or alkaline germs, is state of the art. The production of other finely divided iron oxide or iron oxyhydroxide pigments is also state of the art. Such pigments can contain structures based on α, β, γ, δ, δ ', ε phases and / or Fe (OH) ₂ as well as mixed and intermediate phases thereof. Finely divided yellow iron oxydroxides can be annealed to form finely divided red iron oxides.

The production of transparent iron oxides and iron oxyhydroxides is e.g. B. according to DE A 26 03 050 known from BIOS 1144, pp. 29 to 33 or from FIAT 814, pp. 1 to 26.

Fine-particle yellow iron oxyhydroxide pigments are generally obtained by precipitation of iron (II) hydroxides or carbonates from corresponding iron (II) salt solutions, such as, for. B. FeSO ₄ , FeCl ₂ in pure form or as pickling solutions in the acidic or alkaline pH range and subsequent oxidation to iron (III) oxyhydroxides syn thetized (see below G. Buxbaum, Industrial Inorganic Pigments, VCH Weinheim, 2nd edition, 1998 , P. 231 ff). The oxidation of the divalent to the trivalent iron is preferably carried out with air, and intensive fumigation is advantageous. Oxidation with H ₂ O _{2 also} leads to finely divided iron oxyhydroxides. The temperature during the precipitation and during the oxidation should be chosen as low as possible in order to obtain very finely divided yellow pigments. It is preferably between 15 ° C and 45 ° C. NaOH is preferably used as the alkaline precipitant. However, other precipitants, such as KOH, Na ₂ CO ₃ , K ₂ CO ₃ , CaO, Ca (OH) ₂ , CaCO ₃ , NH ₃ , NH ₄ OH, MgO and / or MgCO ₃ can also be used.

In order to control the precipitated pigments in the direction of the necessary high degree of fineness, the precipitates, e.g. B. of yellow α-FeOOH, as described in the patents US-A 2 558 303 and US-A 2 558 304, carried out in the alkaline pH range with alkali licarbonates as precipitants and generally modifiers added, such as. B. SiO ₂ , zinc, aluminum or magnesium salts, Hydroxicarbonsäu ren, phosphates, metaphosphates. Products so produced are described in US-A 2,558,302. Such germ modifiers do not interfere with the subsequent processing, recycling or other use of the adsorbents according to the invention. In the precipitation processes in the aqueous medium, as far as is known, precipitation in an alkaline environment leads to less hard agglomerated powders than those in an acidic one.

DE-A 42 35 945 reports on the preparation of finely divided iron oxides after a Precipitation process in the acidic pH range and without modifiers.

DE-A 44 34 669 describes a method with which highly transparent yellow, che mix pure iron oxide pigments by post-treating them with sodium hydroxide solution can be produced.

DE-A 44 34 972 reports highly transparent, yellow iron oxide pigments of the α-FeOOH modification with a specific surface area of more than 100 m ² / g with high temperature stability.

DE-A 44 34 973 describes highly transparent yellow iron oxide pigments which have the Process steps germ precipitation in the acidic pH range, germ oxidation, germ maturation and pigment build-up.

Red, transparent iron oxide pigments created by annealing from yellow, transparent Iron oxide pigments are formed from DE-A 44 34 668 and DE-A 42 35 946 known.

The fact that iron oxyhydroxides of different phases in pure form or in any mixture from the known precipitation and oxidation reactions Iron (II) salt solutions are produced, the resulting iron oxyhydroxide, gege optionally after treatment, from the suspension by filtration from the Saline solution separated and largely salt-free, preferably to a residual level ability of <5 mS / cm, the solid or semi-solid filter cake as  it is, or possibly after a mechanical shaping, then one Drying to achieve a solid state is obtained mechanically high-strength material, which has a high binding capacity for the usual wise contains pollutants in waste water or exhaust gases.

Drying is conveniently carried out at temperatures up to 250 ° C. Also a Va vacuum or freeze drying of the material is possible. The grain size of the material is arbitrary, it is preferably between 0.2 and 40 mm, particularly preferred between 0.2 to 20 mm. This can be achieved by mechanical molding Practice the semi-solid, pasty filter cake before drying with a granulating or pelletizing plant or in an extrusion to form bodies with a size in Range between 0.2 and 20 mm and subsequent drying in air a belt dryer or in a drying cabinet, and / or by mechanical Crush to the desired grain size after drying.

Compared to the prior art, the products described are the process for their manufacture and their use for improvement. The granules according to the invention based on finely divided iron (oxi) hydroxides and / or -oxides are in contrast to those from coarse-particle iron oxyhydroxides and / or oxides considerably more resilient and therefore have a much greater abrasion stability against mechanical and hydraulic stress. You can can be used directly as such. Even towards crushing or crushing the next obtained raw dry matter from filter cake or extrusion z. B. can be dispensed with when used in adsorber systems for water purification, since the coarse pieces shred independently when they come into contact with water. This creates a statistical grain size distribution, but no particles of one Size that is appreciable due to the flowing medium from the adsorber be carried out.

On a separate granulation, such as when using conventional iron oxyhydro xiden in the form of (free-flowing) powder would be required, either with the help  non-substance binders or maximum line forces when compacting, can to be completely dispensed with.

According to the invention, the suspensions of the finely divided iron oxyhydroxides or Iron oxides also with ordinary powdered iron oxyhydroxides or iron oxides are added. The respective quantities are determined by the properties Powdered iron oxyhydroxides or iron oxides and those of the invention requirements regarding its mechanical stability and abrasion resistance determined. The addition of powdered pigments is described in generally reduce the mechanical strength of the products according to the invention gladly, however, the filtration of the finely divided suspensions is facilitated. The on The specialist working in the respective field of application is guided by a few Try to determine the optimal mixing ratio for your application can.

The suspensions of the alkaline, finely divided nuclei can also be mixed with an amount of aqueous salts of Fe ³⁺ , Al ³⁺ , Mg ²⁺ , Ti ⁴⁺ or mixtures thereof corresponding to the NaOH excess, so that sufficiently poorly soluble precipitates of Fe (OH) ₃ , Al (OH) ₃ , Mg (OH) ₂ , TiO (OH) ₂ or aging and dehydrated secondary products of the same on the suspended iron oxide and / or iron (oxi) hydroxide particles. It is also possible to react in the opposite way to the iron oxide or iron (oxi) hydroxide particles suspended in Fe ³⁺ , Al ³⁺ , Mg ²⁺ , Ti ⁴⁺ solutions by adding alkalis, such as, for. B. NaOH, Ca (OH) ₂ , KOH, CaCO ₃ , Na ₂ CO ₃ , K ₂ CO ₃ , NH ₄ OH the sparingly soluble precipitates Fe (OH) ₃ , Al (OH) ₃ , Mg (OH) ₂ , TiO (OH) ₂ or their aging and secondary products. The aluminum oxide or aluminum (oxi) hydroxide can also be precipitated from an aluminum suspension (e.g. NaAlO ₂ ) on the iron oxide and / or iron (oxi) hydroxide particles.

The resulting, initially amorphous Fe (OH) ₃ or Al (OH) ₃ ages with time z. B. to the FeOOH or AlOOH phase. This ensures a complete consumption of the sodium hydroxide solution, which was used in excess for the production of the alkaline germ. The materials thus obtained also have high specific surface areas. The material, like the nanoparticulate iron oxydroxides described above, is excellently suitable for use in adsorbers because, in addition to a high adsorption capacity, it also has high stability against mechanical stress.

The granules according to the invention are particularly preferred for cleaning of liquids, especially for removing heavy metals. A preferred application in this technical field is decontamination of water, especially drinking water. In recent times, the removal of Special attention is paid to arsenic from drinking water. The invention Large granules are ideally suited for this purpose, since even the low Authority EPA set limit values through the use of the invention granules are not only adhered to, but can even be undercut.

For this purpose, the granules can be used in conventional adsorber devices, as they currently do, e.g. B. loaded with activated carbon to remove pollutants other types are in use. A batch operation, for example in cisterns or Similar containers, which may be equipped with agitators, are also possible. Use in continuously operated systems such as flow however, adsorption is preferred.

Since raw water to be treated for drinking water is usually also organic ver surface contains impurities such as algae and similar organisms surface of adsorbers, especially the outer surface of granular ad sorbent, during use with mostly mucilaginous deposits that occurs in the water and thus the adsorption of ingredients to be removed severe or even prevent. For this reason, the adsorber devices from Backwashed with water from time to time, which is preferably during low periods Water consumption (see above) on individual devices taken out of operation  is carried out. Here, the adsorbent is whirled up, and by this associated mechanical stress on the surface becomes the undesirable loading was removed and carried out against the direction of flow in commercial use. The Wash water is usually fed to a sewage treatment plant. Here prove themselves the adsorbents according to the invention are particularly good because of their high strength allows cleaning in a short time without significant loss of Ad sorber material would be recorded or the backwash fed to the wastewater water rich in discharged adsorber material, possibly high with Heavy metals.

A suitable pre- and post-filter removes the impurities that the Adsorber cartridge could clog retained.

By the stability of the granules according to the invention and by suitable packing the adsorber granulate minimizes material abrasion.

Spray granules of the iron oxyhydroxide adsorber have proven to be particularly favorable a grain size <2S0 µ has proven itself, because it makes for a particularly good pack lead density.

Since the granules according to the invention are free of foreign binders, this is Material relatively easy to dispose of after use. This is how the adsor Beer arsenic z. B. thermally or chemically removed in special equipment the, and you get an iron oxide pigment as a pure substance, which either for Recycled for the same application or conventional pigment applications gene can be supplied. Depending on the application and legal requirements the adsorber content can also be removed without first removing the heavy metals for example as a pigment for coloring permanent construction materials such as Concrete can be used because the heavy metals extracted from the drinking water permanently immobilized and withdrawn from the water cycle.  

Therefore, there are also water treatment plants or waterworks in which the Granules according to the invention are also operated Ge The subject of the present invention is a method for decontaminating what water using such apparatus and such apparatus itself.

For many applications, especially those in which a maximum mechani cal strength of the granules is not required, the addition of powdered Pigments are preferred in the production of the granules according to the invention Embodiment.

For example, a germ suspension according to Example 2 of the present An notification with up to 40% by weight of commercial goethits (e.g. Bayferrox® 920, Bayer AG, Leverkusen DE) can be added if the obtained invention eats granules to remove arsenic from drinking water flowed adsorbers to be used.

The BET specific surface area of the products according to the invention is determined using the carrier gas method (He: N ₂ = 90: 10) using the single-point method in accordance with DIN 66131 (1993). Before the measurement, the sample is heated for 1 h at 140 ° C in a dry stream of nitrogen.

In order to measure the adsorption of arsenic (III) and arsenic (V), 3 l of an aqueous solution of NaAsO ₂ or Na ₂ HAsO ₄ with the specified concentration of approx. 2 -3 mg / l arsenic were treated with 3 g of the sample to be examined and the bottle was set in motion on rotating rollers. The adsorption rate of As ions on iron hydroxide over this particular period, e.g. B. one hour, is given with mg (As ^{3 + / 5 +} ) / g (FeOOH). H from the difference to the As ^{3 + / 5 +} ions remaining in solution.

To measure the adsorption of Sb ³⁺ , Sb ⁵⁺ , Pb ²⁺ , Hg ²⁺ , Cr ⁶⁺ , Cd ²⁺ ions, the procedure is the same, and the desired concentrations are obtained by dissolving appropriate amounts from Sb ₂ O ₃ , KSb (OH) ₆ , PbCl ₂ , NaCrO ₄ , CdCl ₂ in H ₂ O and adjust the pH to 7-9.

The As, Sb, Cd, Cr, Hg and Pb contents of the loaded iron oxyhydroxide or the solutions are determined by mass spectrometry (ICP-MS) according to DIN 38406-29 (1999) or via optical emission spectroscopy (ICP-OES) according to EN ISO 11885 (1998), each with inductively coupled plasma as an excitation unit.

The mechanical and hydraulic abrasion resistance was assessed according to following method: 10 g of the granules to be examined with grain sizes <0.1 mm were mixed with 150 ml of demineralized water in a 500 ml Erlenmeyer flask and opened a LabShaker shaker (model Kühner, Braun) over a period of time rotated from 30 minutes at 250 revolutions / minute. Subsequently the fraction <0.1 mm was isolated from the suspension using a sieve, dried and weighed. The weight ratio between the weight and the weight is determined the abrasion value in%.

The invention is explained in more detail below with the aid of examples. The bei Games are intended to illustrate the process and are not restrictive represents.

Examples example 1

237 l of an aqueous iron sulfate solution with a concentration of 150 g / l FeSO ₄ were placed at 24 ° C. Then 113 l of an aqueous NaOH solution (227 g / l) were added quickly and the light blue suspension was then oxidized with 40 l of air per hour and mole of iron over 1.5 hours.

The yellow suspension thus obtained was filtered off on a filter press and the Solid washed to a residual conductivity of the filtrate of 1 mS / cm. there was the filter cake as a spreadable and kneadable paste, which on sheets in the area air drying cabinet at 75 ° C to a residual moisture content of 3% by weight was not. The dried material was then broken down into parts sizes between 0.5 and 2 mm. The hard pieces thus obtained were which is used directly in an adsorber tank.

The product consisted of 100% α-FeOOH with an extremely short-needle habit, the needles being stored together in solid macroscopic agglomerates ren. From the scanning electron micrograph z. B. with the enlargement The needle widths of 60,000: 1 were measured by measuring between 15 and 35 nm Needle lengths between 150 and 350 nm determined. The needles were very agglomeration riert.

The BET specific surface area was 122 m ² / g. The adsorption speed with regard to NaAsO ₂ with an initial concentration of 2.3 mg (As ³⁺ ) / l was 2.14 mg (As ³⁺ ) / g (FeOOH) .h, with regard to Na ₂ HAsO ₄ with an initial concentration of 2.7 mg (As ^{5 +} ) / l it was 2.29 mg (As ⁵⁺ ) / g (FeOOH) .h.

Example 2

800 l of an aqueous iron sulfate solution with a concentration of 150 g / l FeSO ₄ were placed at 29 ° C. and 147 l of an aqueous NaOH solution (300 g / l) were added with stirring in 20 minutes. The resulting gray-blue suspension was then mixed with 2.16 kg of a 57% aqueous glycolic acid solution and oxidized for 7 hours with 38 l of air per hour and mole of iron.

The dark brown suspension was filtered off on a filter press and the solid Washed fabric up to a residual conductivity of the filtrate of 1 mS / cm. The filter cake was at 70 ° C in a convection oven to a residual moisture of 5% dried, and the very hard black-brown dry goods were rolled over crushers crushed to grain sizes up to 2 mm. The fine fraction <0.2 mm was over a Sieve separated.

According to the X-ray diffractogram, the product consisted of 100% α-FeOOH from the scanning electron micrograph z. B. with the enlargement of 60,000: 1, the needle widths were determined by measuring between 15 and 20 nm, the needle lengths between 50 and 80 nm. The particles were very agglomerated. The BET specific surface area was 202 m ² / g. The granules thus obtained were filled directly into an adsorber tank without further treatment.

The granules showed an excellent adsorption behavior for the in the flowing water contained pollutants and showed a high Abriebfefe stability, especially while the adsorber tank is being backwashed and as a result the granules are whirled up. The abrasion value was 30 minutes only 1%.

adsorption

The adsorption rate compared to NaAsO ₂ with an initial concentration of 2.4 mg (As ³⁺ ) / l was 1.0 mg (As ³⁺ ) / g (FeOOH) .h, compared to Na ₂ HAsO ₄ with an initial concentration of 2.8 mg (As ⁵⁺ ) / l it was 2.07 mg (As ³⁺ ) / g (FeOOH) .h.

Example 3

An α-FeOOH suspension obtained according to Example 2 was after two hours of rubbing at 30 ° C. with stirring with 1.3 l of an aqueous 300 g / l NaOH solution and at the same time post-oxidized with 190 l of air for one hour. The product was worked up as described in Example 2. Finely divided needles made of pure α-FeOOH with a BET specific surface area of 130 m ² / g were produced. From the scanning electron micrograph z. B. with the enlargement of 60,000: 1, the needle widths were determined by measuring between 15 and 20 nm, the needle lengths between 50 and 90 nm. The needles were very agglomerated. The granules proved to be mechanically and hydraulically very stable, the abrasion value was only 3.9%.

adsorption

The adsorption rate against NaAsO ₂ with an initial concentration of 2.3 mg (As ³⁺ ) / l was 1.1 mg (As ³⁺ ) / g (FeOOH). H, compared to Na ₂ HAsO ₄ with an initial concentration of 2.8 mg (As ⁵⁺ ) / l it was 1.7 mg (As ³⁺ ) / g (FeOOH) .h.

Example 4

306 l of an aqueous NaOH solution (45 g / l) were initially introduced at 31 ° C. and 43 l of an aqueous solution of FeCl ₂ (344 g / l) were added rapidly while stirring and then 60 l of air per hour and mole Fe oxidized. The dark yellow suspension thus obtained was worked up as described in Example 1.

According to the X-ray diffractogram, the product consisted of 100% α-FeOOH. From the scanning electron micrograph z. B. with the enlargement of 60,000: 1, the needle widths were determined by measuring between 15 and 50 nm, the needle lengths between 100 and 200 nm. The needles were very agglomerated. The specific BET surface area was 132 m ² / g.

The granules thus obtained were placed in an adsorber tank without further treatment filled. The granules showed an excellent adsorption behavior for the im Water contained pollutants and showed a high abrasion resistance, in particular re while the adsorber tank is backwashed and consequently the granules are strong be whirled up. The abrasion value was only 12% by weight after 30 minutes.

adsorption

The adsorption rate against NaAsO ₂ with an initial concentration of 2.4 mg (As ³⁺ ) / l was 2.11 mg (As ³⁺ ) / g (FeOOH). H, compared to Na ₂ HAsO ₄ with an initial concentration of 2.7 mg (As ⁵⁺ ) / l it was 2.03 mg (As ⁵⁺ ) / g (FeOOH) .h.

Example 5

124 l of an aqueous NaOH solution (114 g / l) were introduced at 24 ° C. and 171 l of an aqueous solution of FeSO ₄ (100 g / l) were added rapidly while stirring and then 10 l of air per hour and mole Fe oxidized. Immediately after full oxidation, 56 l of an aqueous solution of Fe2 (SO ₄ ) ₃ (100 g / l) were added and the mixture was stirred for 30 minutes. The yellow-brown suspension thus obtained was worked up as in Example 1.

According to the X-ray diffractogram, the product consisted of 100% α-FeOOH. From the scanning electron micrograph z. B. with the enlargement of 60,000: 1, the needle widths were determined by measuring between 15 and 35 nm, the needle lengths between 70 and 180 nm. The needles were very agglomerated. The BET specific surface area was 131 m ² / g. The abrasion value was only 7% by weight after 30 minutes.

adsorption

The adsorption rate with respect to NaAsO ₂ with an initial concentration of 2.3 mg (As ³⁺ ) / l was 1.7 mg (As ³⁺ ) / g (FeOOH). H, with respect to Na ₂ HAsO ₄ with an initial concentration of 2.7 mg (As ⁵⁺ ) / l it was 1.2 mg (As ⁵⁺ ) / g (FeOOH) .h.

Example 6

7905 kg of FeSO _{4 were} introduced, dissolved to a volume of 53.3 m ³ with water, the solution was cooled to 14 ° C. and 1000 kg of MgSO ₄ .7 H ₂ O were added to this solution. The template is then diluted at 14 ° C with 5056 kg NaOH as a solution with approx. 300 g / l and then oxidized with 4000 m ³ / h air to a degree of precipitation of <99.5%. The mixture was washed on a filter press until the residual conductivity of the filtrate was <1000 µS / cm and the paste was pressed through a perforated plate with a hole diameter of 7 mm and thus formed into strands. The strands are dried on a belt dryer to a residual moisture of approx. 3%. According to the X-ray diffractogram, the product consists of 100% α-FeOOH with very short needles. From the ra electron micrograph z. B. with the magnification of 60,000: 1, the needle widths were determined by measuring between 30 and 50 nm. The needle lengths could not be clearly determined because the needles were too agglomerated. The BET specific surface area was 145 m ² / g. The abrasion value was only 6% after 30 minutes.

adsorption

The adsorption rate with respect to NaAsO ₂ with an initial concentration of 2.5 mg (As ³⁺ ) / l was 1.8 mg (As ³⁺ ) / g (FeOOH). H, with respect to Na ₂ HAsO ₄ with an initial concentration of 2.9 mg (As ⁵⁺ ) / l it was 1.5 mg (As ⁵⁺ ) / g (FeOOH). h.

Example 7

4096 kg of NaOH (as a solution with approx. 300 g / l) were introduced and diluted to 40 m ³ with water. 4950 kg of FeSO ₄ are dissolved with water to give a 48.5 m ³ solution, cooled to 15 ° C. and then pumped to the NaOH receiver in 1 h. The suspension was then oxidized with 1500 m ³ / h air in about 2 h. Approximately 2 m ^{3 of} the germ suspension was washed on a filter press to a filtrate conductivity <1000 μS / cm, the filter cake was dried at 75 ° C. in a drying cabinet and the dried material was crushed to grain sizes <1.5 mm. The fine fraction <0.5 mm was separated off via a sieve. The material thus obtained had a BET specific surface area of 153 m ² / g and consisted 100% of α-FeOOH. From the scanning electron micrograph z. B. with the enlargement of 60,000: 1, the needle widths were determined by measuring between 15 and 35 nm, the needle lengths between 50 and 100 nm. The needles were very agglomerated.

adsorption

The adsorption rate with regard to NaAsO ₂ with an initial concentration of 2.7 mg (As ³⁺ ) / l was 1.7 mg (As ³⁺ ) / g (FeOOH). H, with respect to Na ₂ HAsO ₄ with an initial concentration of 2.8 mg (As ⁵⁺ ) / l it was 1.4 mg (As ⁵⁺ ) / g (FeOOH) .h.

Example 8

1600 g of the alkaline germ suspension (2.7% FeOOH) prepared according to Example 7 were mixed with an aqueous solution of FeSO ₄ (100 g / l) at room temperature while stirring, with simultaneous gassing with 130 l / h of air to pH 8. The germ suspension obtained is filtered, washed and the filter cake is dried at 75 ° C. and, as in Example 7, crushed to a particle size between 0.5 and 2 mm. The material thus obtained had a BET specific surface area of 163 m ² / g and, according to the X-ray diffractogram, consisted of 100% of α-FeOOH. From the scanning electron micrograph z. B. with the enlargement of 60,000: 1 it could be seen that the needles are highly agglomerated.

adsorption

The adsorption rate for NaAsO ₂ with an initial concentration of 2.7 mg (As ³⁺ ) / l was 2.0 mg (As ³⁺ ) / g (FeOOH) .h, for Na ₂ HAsO ₄ with an initial concentration of 2.7 mg (As ⁵⁺ ) / l it was 1.9 mg (As ⁵⁺ ) / g (FeOOH). h, at KSb (OH) ₆ (starting concentration 3.0 mg (Sb ⁵⁺ ) / l) the adsorption was 2.5 mg (Sb ⁵⁺ ) / g (FeOOH) .h, with regard to Na ₂ CrO ₄ (initial concentration 47 µg (Cr ⁶⁺ ) / l) 42 µg (Cr ⁶⁺ ) / g (FeOOH) .h were adsorbed, with PbCl ₂ (initial concentration 0.94 mg (Pb ^{2 +} ) / l, 0.46 mg (Pb ²⁺ ) / g (FeOOH) .h was adsorbed.

Example 9

6.4 l of an aqueous solution of NaOH (100 g / l) were initially introduced at 29 ° C. with stirring, and 12.2 l of an aqueous iron (II) sulphate solution (100 g / l) up to pH 9 were added while simultaneously supplying air. The suspension thus obtained was worked up as in Example 1. The material had a BET specific surface area of 251 m ² / g and, according to the X-ray diffractogram, consisted 100% of α-FeOOH. The scanning electron microscope image shows short, stubby needles that agglomerate strongly. Abrasion behavior: 5%.

adsorption

The adsorption rate with regard to NaAsO ₂ with an initial concentration of 2.7 mg (As ³⁺ ) / l was 1.1 mg (As ³⁺ ) / g (FeOOH). H, with respect to Na ₂ HAsO ₄ with an initial concentration of 2.7 mg (As ³⁺ ) / l it was 1.0 mg (As ⁵⁺ ) / g (FeOOH) .h.

Example 10

4096 kg of NaOH (as a solution with approx. 300 g / l) were introduced and diluted to 40 m ³ with water. 4950 kg of FeSO ₄ are dissolved with water to give a 48.5 m ³ solution, cooled to 15 ° C. and then pumped to the NaOH receiver in 1 h. The suspension was then oxidized with 1500 m ³ / h air in about 2 h. Approximately 87 m ^{3 of} this suspension were mixed with 14.4 m ³ FeClSO ₄ solution (113.4 g / l) while stirring and stirred for 30 min. The mixture was washed on a filter press until the filtrate had a residual conductivity of <1000 µS / cm and the paste was pressed through a perforated plate with a hole diameter of 7 mm and formed into strands. The strands are dried on a belt dryer to a residual moisture of approx. 5%. The dry pellets were crushed to a grain size of 2 mm. The material thus obtained had a BET specific surface area of 142 m ² / g and consisted 100% of α-FeOOH. From the scanning electron micrograph z. B. with the enlargement of 60,000: 1, the needle widths were determined by measuring between 15 and 50 nm, the needle lengths between 10 and 150 nm. The needles were very agglomerated.

adsorption

The adsorption rate with respect to NaAsO ₂ with an initial concentration of 2.7 mg (As ³⁺ ) / l was 2.1 mg (As ³⁺ ) / g (FeOOH). H, with respect to Na ₂ HAsO ₄ with the initial concentration of 2.8 mg (As ⁵⁺ ) / l it was 2.0 mg (As ⁵⁺ ) / g (FeOOH). h, with respect to CdCl ₂ (starting concentration 2.7 mg (Cd ²⁺ ) / l) the adsorption was 1.1 mg (Cd ²⁺ ) / g (FeOOH) .h, with respect to KSb (OH) ₆ (initial concentration 2.6 mg (Sb ⁵⁺ ) / l it was 1.9 mg (Sb ⁵⁺ ) / g (FeOOH) .h, with regard to Sb ₂ O ₃ (initial concentration 2.3 mg (Sb ³⁺ ) / l, it was 2.0 mg (Sb ³⁺ ) / g (FeOOH) .h, with respect to Na ₂ CrO ₄ (starting concentration 2.6 mg (Cr ⁶⁺ ) / l, it was 1.1 mg (Cr ⁶⁺ ), with respect to PbCl ₂ (initial concentration 1.6 mg (Pb ²⁺ ) / l it was 1.57 mg (Pb ²⁺ ) / g (FeOOH). H.

Example 11

569 ml of a MgSO ₄ solution (100 g / l) were added to 1 l of a suspension of Bayferrox © 920 with a solids content of 50 g / l FeOOH, then 173 g of a 24% NaOH solution were added with stirring and 15 min stirred. The yellow suspension is washed on a suction filter to a residual conductivity of the filtrate of 1 mS / cm, the filter cake is dried at 75 ° C. in a drying cabinet to a residual moisture of <2%. The product was granulated to grain sizes between 0.5 and 2 mm and the granules were used for arsenic adsorption.

According to the X-ray diffractogram, the product consists of α-FeOOH and Mg (OH) ₂ . From the scanning electron micrograph z. B. with the magnification of 60,000: 1 you can see that the needles of the α-FeOOH type of amorphous layers are glued together or agglomerated. The specific surface area according to BET was 43 m ² / g and was thus compared to Bayferrox © 920 (BET approx. 15 m ² / g). The abrasion value was only 11% after 30 minutes.

The adsorption rate for an aqueous NaAsO ₂ solution with an initial concentration of 2.6 mg (As ³⁺ ) / l was 1.2 mg (As ³⁺ ) / g (FeOOH). H, for an Na ₂ HAsO ₄ solution with an initial concentration of 2.7 mg (As ⁵⁺ ) / l was 1.5 mg (As ⁵⁺ ) / g (FeOOH) .h.

Example 12

950 g of a suspension of an alkaline nanoparticle germ of α-FeOOH (solids content: 5.26 g / l FeOOH, 1.14%% NaOH) were stirred with 46 ml of an Al ₂ (SO ₄ ) ₃ solution (100 g / l Al ₂ O ₃ ) and stirred for 15 minutes. The brown suspension is washed on a suction filter to a residual conductivity of the filtrate of 1 mS / cm, the filter cake is dried at 75 ° C. in a drying cabinet to a residual moisture of <2%. The product was granulated to grain sizes between 0.5 and 2 mm and the granules were used for arsenic adsorption.

In the X-ray diffractogram of the product, only α-FeOOH was detected, which, as can be seen from the rater electron micrograph, is present as very short and strongly agglomerated needles. The BET specific surface area was 102 m ² / g. The abrasion value was only 5% after 30 minutes.

The adsorption rate for an aqueous NaAsO ₂ solution with an initial concentration of 2.6 mg (As ³⁺ ) / l was 2.0 mg (As ³⁺ ) / g (FeOOH) .h, for an Na ₂ HAsO ₄ solution with an initial concentration of 2.1 mg (As ⁵⁺ ) / l was 1.5 mg (As ⁵⁺ ) / g (FeOOH) .h.

Embodiment 13

Adsorber granules shown according to Examples 1-12, typically between 0.5 and 2 mm or in comminuted form, are stored in a contact space shown in FIG. 1 or 2. The filtration unit has a flow rate for air as fluid of 2000 ml per minute at a pressure difference of 0.1 bar.

Claims (28)

1. Media flowable filtration units for removing pollutants from fluids, consisting of a cartridge housing ( 4 ), which consists of a container that centers an inlet pipe ( 6 ) in the center, opposite flat filter layers ( 3 ), ( 10 ), one Lid, which ensures the inlet ( 1 ) and outlet ( 12 ) of the fluid to be cleaned, as well as a bottom part ( 9 ), characterized in that the filter cartridge housing ( 4 ) protects the agglomerates of finely divided iron oxide and / or iron oxyhydroxide contains in lumpy form, the finely divided iron oxide and / or iron oxide hydroxide having a BET surface area of 50 to 500 m ² / g, preferably 80 to 200 m ² / g, the agglomerates optionally iron oxide pigments having BET surfaces below the above limits may contain, the content of these is at most so high that the strength of the feed compared to the forces acting on it of the flowing medium is so large that the loading of the feed by the flowing medium does not lead to undesired abrasion of the feed material, such that the fluid to be cleaned is intended to clean the inlet connection ( 1 ), the inlet pipe ( 6 ), the strainer basket ( 7 ) , possibly filter material ( 8 ) in the floor space ( 9 ), the lower frit plate ( 10 ), then the adsorber material ( 5 ) in the contact space ( 4 ), the upper frit plate ( 3 ), the lid space with filter material ( 2 ) and then over the Outlet nozzle leaves the outlet pipe ( 12 ). 2. Filtration unit according to claim 1, characterized in that the housing seraum ( 4 ) from the lid ( 13 ) and / or from the bottom part ( 9 ) can be separated by a plug or screw connection. 3. Filtration unit according to claim 1-2, characterized in that the inlet tube can be removed from the cartridge housing.   4. Filtration unit according to claims 1-3, characterized in that the flat filter systems ( 3 , 10 ) for the removal of pollutants from gases consist of hydro phobic membranes. 5. Filtration unit according to claim 4, characterized in that the hydrophobic ben membranes are made of polytetrafluoroethylene. 6. Filtration unit according to claims 1-3, characterized in that the flat filter systems ( 3 , 10 ) for the removal of pollutants from aqueous solutions consist of hydrophilic membranes. 7. Filtration unit according to claim 6, characterized in that the hydrophi len membranes represent membrane adsorbers. 8. Filtration unit according to claims 3-7, characterized in that the Membranes have a pore diameter in the range from 0.2 to 0.5 µm, preferably have of 0.2 µm. 9. Filtration unit according to the preceding claims, characterized in that at least one of the flat filter layers ( 3 , 10 ) is supported on one or both sides. 10. Filtration unit according to the preceding claims, characterized in that the lid contains a valve for escaping gases.   11. Filtration unit according to the present claims, characterized in that the housing space ( 4 ) is designed as a truncated cone. 12. Filtration unit according to the preceding claims, characterized in that the flow is reversed in the manner described in claim 1. 13. Apparatus according to claims 1-12, characterized in that it is in the Media is liquids. 14. Apparatus according to claims 1-12, characterized in that it is the Media is about water. 15. A process for the production of agglomerates of finely divided iron oxide and / or iron oxyhydroxide in lumpy form, characterized in that firstly an aqueous suspension of finely divided iron oxides and / or iron oxyhydroxides with a BET surface area of 50 to 500 m ² / g, preferably of 80 up to 200 m ² / g, in a manner known per se and then removing the water and components dissolved therein by:
either
initially only the water, preferably by evaporation, is removed from the suspension and the residue thus obtained is redispersed in water, the suspension obtained is filtered, the residue is washed preferably salt-free, the filter cake obtained as residue is completely or dewatered and the material thus obtained is converted into the desired Shape and / or size crushed or partially dewatered to obtain a sufficiently solid state and the paste thus obtained is subjected to shaping and subsequent further drying to obtain a lumpy state
or
the suspension is filtered and the residue is washed with low salt, the filter cake in the form of a solid to semi-solid paste, which is obtained as a residue, either completely dewatered and the material thus obtained is then comminuted to the desired shape and / or size or partially to obtain a sufficiently solid one Condition dewatered and the paste thus obtained is subjected to shaping and subsequent drying to obtain a lumpy condition
and optionally subjecting the material thus obtained to further grinding or grinding. 16. A method for producing an adsorbent / reactant, characterized in that

• a) aluminum, magnesium, and / or titanium oxides or (oxi) hydroxides or their aging and dehydrated secondary products are mixed into an aqueous suspension of iron oxide and / or iron oxyhydroxide, including Fe (OH) ₂ , and then
• b) either the suspension is dried to obtain a solid state and the solid material is then mechanically comminuted to the desired shape and / or size or
• c) the suspension is optionally subjected to mechanical shaping after predrying in the semi-solid state and subsequent (further) drying to obtain a solid state.

17. The method according to claim 15 and 16, characterized in that the iron oxide and / or iron oxyhydroxide structures based on α-, β-, γ-, δ-, δ'-, ε- and / or Fe (OH ) ₂ phases, ferrihydrite and mixed and intermediate phases of the same. 18. The method according to claims 15 and 16, characterized in that in addition or iron carbonates instead of the iron oxide and / or iron oxy hydroxides be set. 19. The method according to claims 15 and 16, characterized in that the iron oxide and / or iron oxyhydroxides with oxides and / or (oxi) hydroxides Elements Fe, Al, Mg, Ti are solidified. 20. The method according to claims 15 to 19, characterized in that as iron oxides and / or iron (oxi) hydroxides commercially available pigments are used. 21. The method according to claims 15 to 19, characterized in that as iron oxide and / or iron (oxi) hydroxide transparent pigments are used. 22. The method according to claims 15-21, characterized in that for precipitation the Al, Mg or Ti oxides and / or (oxi) hydroxide salts from the series of Carbonates, chlorides, fluorides, nitrates, sulfates, sulfites can be used.   23. Use of agglomerates obtainable according to claims 15-22 in Appa rates and investments according to claims 1 to 14. 24. Use of agglomerates obtainable according to claims 15-22 for Rei of gases. 25. Use of agglomerates obtainable according to claims 15-22 for Rei cleaning liquids. 26. Use of agglomerates obtainable according to claims 15-22 for what preparation. 27. Use of agglomerates obtainable according to claims 15-22 for ent removal of heavy metals, as well as phosphorus, antimony, beryllium, selenium, Tellurium and cyano compounds from water. 28. Use of agglomerates obtainable according to claims 15-22 for ent removal of arsenic compounds from water.