DE19927907A1 - One stage high density sludge purification of acidic waste water from mining operations to remove uranium, iron, sulfate ions and other impurities - Google Patents

Abstract

A process and apparatus are claimed for one-stage high density sludge purification of waste water from mining operations having pH 2-4 and containing metal ions such as Fe as well as up to 50g/l uranium or its products and up to 5g/l sulphate. Purification by a one-stage high density sludge (HDS) method of water of pH 2-4 from mining operations and containing metal ions such as Fe as well as up to 50g/l uranium or its products and up to 5g/l sulphate comprises (i) adding a precipitating agent (6) and/or BaCl2 by spraying the water from a chamber (2) via nozzle(s) (3), operating together with an atomizer on the water-jet pump principle, into the first chamber (10) of a multichamber vessel (9); (ii) simultaneously feeding into chamber (10) the recycled washed ore sludge (5) which has been previously mixed in a conditioning tank (8) with the precipitating agent (6), the sludge stream and the contaminated water (aereated during its free fall) being held in chamber (10) for 10-30 minutes for Fe and Mn oxidation before overflowing in tube (13); (iii) feeding each chamber (10) with precipitating agent and aereated contaminated water and raising the pH stagewise in increments of 1.0-2.5 to 7.0-8.5 so that addition of BaCl2 to the vessel (9) causes co-precipitation of radium; (iv) effecting solid/liquid separation by adding flocculant in a stable suspension bed of metal hydroxide-gypsum in a high capacity concentrator (14); (v) recycling for more than 10 times most of the drawn-off sludge (16) (controlled by the sludge level (18)) to the process and renewing pH alteration by addition of precipitating agent (6) and mixing with contaminated water; and (d) directly disposing of the remaining easily dewatered inorganic sludge residue. There is also an Independent claim for apparatus for purifying acidic, Fe- and sulfate-containing waste water from mining operations by use of earthen or concrete vessels and a clarifier or round concentrator, the apparatus comprising a distributing chamber (4) above a partitioned multichamber vessel; a distributor (2) with one or more nozzles (3) with different lengths and of inlet : outlet diameter ratio 1.5-2.5 : 1; an atomizer on each nozzle with air inlet openings and/or internal atomizing lattice; a bank of \-2 aereating chambers (10) fed by the water-jet principle and of sufficient volume to allow the required dwell time; overflows (11) between the chambers; a narrow inlet tube (12) into a tube (13) which has a constriction just before its outlet end; and a concentrator (14) with cross-sectional area ratios inlet tube (12) (A0) : tube (13) (A1) : constriction (A2) : tube (13) outlet (A3) : concentrator (14) (A4) = 0.05-0.2 : 1 : 0.3-0.7 : 0.5-0.9 : 5-9, the upper slud ge level varying between 1.5m above the outlet of tube (13) and 0.5m below the clear water overflow (17) and the value of cross-sectional area (A4) of the concentrator being adjusted to the required through-flow for the plant.

Description

The invention relates to a method and an apparatus for cleaning acidic, iron and mining waters containing sulfate, which are caused by increased concentrations of uranium up to 50 mg / l, its secondary products, a high sulfate content up to 5 g / l, rock-specific metal ions, especially iron, and a low pH between 2 and 4 are characterized. These mining waters to be cleaned fall in particular when flooding mines which were mined using sulfuric acid leaching of the ore-containing rock or by oxidation of sulfidic ores.

The cleaning of almost neutral mining water with the separation of uranium and radium compounds is known from DE 43 22 663 A1. An organic polymer aggregate with amidoxime and hydroxamic acid structures is used, which is known from DE 40 16 543 A1. Both the low pH value in the inlet as well as the accumulation of organic precipitation sludge and the introduction of chloride ions into the process (via FeCl ₃ additions) make this process practically unsuitable.

DE 43 13 127 A1 proposes the separate separation of arsenic, uranium and radium from mining water using hydrogen peroxide, iron (III) ions, phosphoric acid and milk of lime. In addition to the considerable entry of chloride and phosphate into the process, the pH must be adjusted twice with lime milk, so that an overall high chemical consumption (up to 200 g / m ³ phosphorus and up to 280 g / m ³ chloride) is required.

DE 43 07 468 A1 proposes the components of building rubble to bind Why use uranium and other contaminants in mining remediation waters? with high uranium concentrations up to 220 g rubble per liter of water to be cleaned required are. With this method, there are also considerable amounts of rubble, that have to be disposed of and deposited.

The use of sulfides to separate radioactive heavy metals is discussed in DE 27 14 202 C2 described and also in practice for cleaning heavy metal containing Watering the Pit Drainage (Larsen, H. P .; Ross, L. W .: Operating Handbook of Mineral Processing, 1976, p. 349). The use of sulfides is because of them  water-polluting properties are problematic and requires the use of additional precipitants for setting the excess sulfide.

The treatment of acidic, metal-containing water with calcium hydroxide is generally known. where hydroxides of many metals can be precipitated. In the NUREG / CR-3906 report, PNL-5179 (Opitz, B.E .; Dodson, M.E .; Serne, R.J .: Pacific Northwest Laboratory, Richland, WA, May 1985) laboratory experiments on the alternative use of calcium hydroxide, Calcium carbonate and a mixture of calcium hydroxide and sodium bicarbonate Precipitation of the components of acidic, uranium-containing water from processing plants and waste Settling basin described. Disadvantages of this method are in addition to the need for large ab settling basin for the implementation of the process, the high effort involved in clearing / removing sludge care and the formation of gypsum incrustations.

In the practice of iron ore mining, the so-called HDS method (high Density Sludge) used to treat mining water to be cleaned. The specifics of this The method is that the gypsum-containing precipitation sludge from thickeners in the Inlet of the neutralizing agent are recycled.

Treatment of mining water with lime for the precipitation of iron hydroxide and brains their subsequent sedimentation in open earth or concrete pools, inclined clarifiers or Circular thickening with a scraper is one of the standard techniques for water purification (Hartinger, L .: Handbook of wastewater treatment for the metalworking industry. Hanser Verlag Munich, Vienna 1976; Hartinger L .: Handbook of sewage and Recycling technology. Hanser Verlag Munich, Vienna 1995; Teaching and manual of the Sewage technology. 3rd Edition; Verlag Ernst &Sohn; Berlin 1983; Graef, R .; Hartinger, L .; Lohmeyer, S .; Schwering H.-U .: Waste water technology in production - WEKA practice manual. WEKA specialist publishing house, Augsburg 1993/1999).

The achievable surface loads of the sedimentation basin are generally less than 0.5 m ³ / (m ² h), which results in high expenses for the construction of large basins as well as for sludge clearing and dewatering.

The invention has for its object an effective, inexpensive method with minimized use of water-polluting substances as adsorbents or precipitants, constant cleaning effects over a longer period of time, high degree of cleaning for uranium and its secondary products and with a simple and reliable device for cleaning Develop mining waters with the following advantages:

• - high area throughput and thus relatively small dimensions of the thickener,
• - low chemical consumption,
• - good drainability of the sludge and
• - Extensive avoidance of gypsum encrustations on system parts.

At the same time, the residues are harmless to the environment and with little pollution of the Dispose of operating personnel as well as one that corresponds to the specified limit values To deliver pure water to the receiving water.

This object is achieved in that the mining water with respect to uranium, its secondary products and / or sulfate and metal contaminations is cleaned in a one-step process according to the HDS method with the addition of lime milk and / or barium chloride as precipitant, the one to be cleaned Raw water from a distribution box via one or more inlet nozzles, which work in conjunction with an atomizer according to the water jet pump principle, falls freely into the first chamber of the multi-chamber reaction basin. At the same time, the recycled sludge return, which was previously mixed with precipitant in a conditioning tank, is introduced into the first chamber, the raw water aerated by the free fall and the recycled sludge return for iron and manganese oxidation with an average time of 10 to 30 minutes each Chambers of the multi-chamber reaction tank dwell in the guide tube before overflow, each chamber being fed separately with precipitant, with further aeration of the raw water, and the pH value in steps of 7.5 to 8.5 in increments ΔpH of 1 with respect to the pH value by metering the precipitant is increased to 2.5. By adding barium chloride (BaCl ₂ ) to the multi-chamber reaction basin, the co-precipitation of radium from the raw water to be cleaned takes place, the solid / liquid separation with the addition of flocculation aids in a stable floating bed made of metal hydroxide gypsum particles (flakes) in one High-performance thickener runs out, the majority of the precipitated sludge drawn off at the sludge outlet of the high-performance thickener during control and regulation of the sludge level in the process with renewed, pH-controlled addition of precipitant and mixture with the raw water is recycled more than 10 times and the proportion of the withdrawn from the process easily drained, inorganic precipitation sludge is disposed of without intermediate storage.

By recycling the precipitate more than 10 times at the sludge outlet, it becomes easy drainable metal hydroxide gypsum sludge, which contains the precipitated uranium and compounds its follow-up products, with a solid content of over 10 M% at continuous deduction and up to more than 30 M% with discontinuous discharge.

The resulting inorganic precipitation sludge is immobilized with conventional binders and after hardening, an immobilizate of high strength and low elutability becomes a closed pollutants deposited under real elution conditions.

The device for carrying out the process for cleaning acidic, iron and sulfate-containing mining water is designed according to the invention so that the inflow of the mining water to be cleaned from a distribution box above the multi-chamber reaction basin in free fall via one or more inlet nozzles with different lengths, due to different integration lengths of the inlet nozzles in the distribution box, the diameter of the inlet nozzle in relation to the inlet diameter of the inlet nozzle: outlet diameter of the inlet nozzle being equal to 1.5 to 2.5: 1 and at the outlet of each inlet nozzle an atomizer with air inlet openings and / or an atomizer grille being fitted inside , in the first chamber of the multi-chamber reaction basin according to the water jet pump principle, the multi-chamber reaction basin consists of at least two chambers to be aerated, the volume of the respective chamber by the required dwell time of the z u raw water is determined, and the overflows between the chambers in the partition walls are staggered, that the cross-sectional areas of the inlet pipe, the guide pipe, which has a constriction just before the outlet, and the high-performance thickener in the ratio of the cross-sectional area of the inlet pipe (A ₀ ): Cross-sectional area of the guide tube (A ₁ ): Cross-sectional area of the guide tube at the constriction (A ₂ ): Cross-sectional area of the guide tube at the outlet (A ₃ ): Cross-sectional area of the high-performance thickener (A ₄ ) equal to 0.05 to 0.2: 1: 0, 3 to 0.7: 0.5 to 0.9: 5 to 9, the upper sludge level fluctuating between at least 1.5 m above the trailing edge of the guide tube to 0.5 m below the overflow edge of the clear water drain and the absolute size of the The cross-sectional area of the high-performance thickener (A ₄ ) must be adapted to the target throughput of the system.

A constant level of the mining water to be cleaned in the distribution box is regulated by the number of inlet nozzles, the dimensioning of the inlet diameter (D ₃ ) of the inlet nozzle and the outlet diameter (D ₄ ) of the inlet nozzle as well as the different embedment lengths (L _e ) of the inlet nozzles.

The principle of the method and the device for cleaning the mining water shows Scheme 1.

Scheme 1

Outline of the procedure

The method and the device are characterized by:

• - The solid / liquid separation takes place in a stable floating bed made of metal hydroxide gypsum particles. This means that the suspension flowing into the high-performance thickener is evenly distributed among the working zone. During the ascent, the sludge bed zone is passed, the solid is decelerated and fine constituents are adsorbed on the particles of the floating bed. Only sufficiently large flakes sediment from the floating bed into the compression zone. The mode of action is thus characterized as a coupling of filtration and sedimentation.
  In this filtration and sedimentation process, up to 95% of the uranium and its by-products are removed from the water to be cleaned and firmly bound to the sedimenting flakes.
• - New is the coupling of the HDS method with a solid / liquid separation after the high performance thickener principle. By the ratio of the cross-sectional areas of the discharge tube, the guide tube and the high-performance thickener, the floating bed is generated and at the same time achieved a high area throughput.
• - The sludge return is conditioned before being fed into the multi-chamber reaction tank. The high-performance thickener is constantly 10 to 20 times the amount of the newly formed Sludge removed and recycled. Only 5 to 10% of the resulting sludge will be removed from the process. The recycled sludge return is in the so-called Conditioning tank mixed intensively with the precipitant, oversaturated and only afterwards fed to the multi-chamber reaction tank. The precipitant is dosed via the pH value of the conditioning tank controlled. This means that the formation of solid particles occurs predominantly the supersaturated solid surface and not on parts of the apparatus (gypsum encrustation), d. H. the increased discharge of uranium and its secondary products remains on the particles of the Metal hydroxide gypsum slurry bound.
• - Radium is precipitated in the multi-chamber reaction tank by adding barium chloride (BaCl ₂ ), whereby the high sulfate content of the raw water leads to co-precipitation of the radium with barium sulfate and the barium discharge into the pure water is negligible. The benefits of full chemical use due to sludge recycling also apply to barium chloride.
• - The setting of a stationary sludge floating bed in the high-performance thickener enables light the realization of a continuous sludge removal from the process. Without yet Repeated interim storage can be done after recycling the precipitate more than 10 times and a continuous sludge drain, an easily drainable metal hydroxide gypsum Sludge with a solids content of over 10 M% or up to over 30 M% with discounts Nuclear sludge removal using decanters and thick matter pumps and lines up to Remove the place of storage of the felling sludge (pile of waste). This eliminates the work intensive processes of sludge removal from sedimentation tanks and sludge watering with filter press.
• - By mixing the resulting inorganic precipitation sludge with a conventional bandage medium (cement, hydrated lime, ashes, etc.) can be stored directly at the place of storage mechanically stable, purely inorganic immobilizate are generated in which the radioactive  and other pollutants are permanently and elution-stable included. Before leaving the property will be hardened to the place of its final storage (waste dump) promotes and deposits.
• - Via the inlet pipe, the tangential entry of the mining water to be cleaned from the multi-chamber reaction basin into the guide pipe takes place, so that the considerable inlet speed (v ₀ ) converts into a rotational movement of the liquid, while the vertical speed component v ₁ = Q _R / A ₁ in the guide tube practically results from the raw water intake per unit time (Q _R ) and the cross-sectional areas of the guide tube (A ₁ ). Because of the ratio of the cross-sectional areas A ₀ : A ₁ 0.05 to 0.2: 1, there is a sharp reduction in the mean vertical speed component (v ₁ ) in the guide tube, the guide tube reaching at least 1.5 m below the sludge level. A constriction in the guide tube increases the vertical speed component (v ₂ ) in the narrowest point of the guide tube to v ₂ = v ₁ (A ₁ / A ₂ ) at a ratio of A ₁ : A ₂ = 1: 0.3 to 0.7 and subsequently receives a radial speed component by expanding the cross section to A ₃ at a ratio of A ₁ : A ₃ = 1: 0.5 to 0.9. Supported by an impact cone and the dynamic pressure of the medium in the lower part of the high-performance thickener, the direction of movement of the mining waters is reversed and, due to the large cross-sectional expansion, the vertical speed component is reduced to v ₄ = v ₁ (A ₁ / A ₄ ) at a ratio from A ₁ : A ₄ = 1: 5 to 9.
• - The functionality of the high-performance thickener is based on the fact that the average ascent rate (v ₄ ) is lower than the sink rate (v ₅ ) of the particles of the mud bed. This creates a floating bed zone in which the metal hydroxide-gypsum particles carried by the mining water to be cleaned are filtered, so that a relatively sharp horizontal boundary between sludge (solid) and clear water is formed.
• - Depending on the composition and concentration of the pollutants in the raw water, the concentration of flocculants and the neutralization process, the high-performance thickener can have a surface load of 1 to 10 m ³ / m ² h (throughput is the throughput [m ³ / h] per Unit area (m ² ), ie it corresponds to the ascent rate v ₄ (m / h]) If the sink rate (v ₅ ) of the metal hydroxide gypsum particles is known, the dimensioning of the device can be determined, the sink rate (v ₅ ) even in a complex manner depends on both the medium to be cleaned and the neutralization technology.
• - The height of the floating bed zone or the sludge level (H _S ) above the exit edge of the guide tube is at least 1.5 m in order to achieve very good filtration of the clear water and solids contents above 10 M% with continuous removal. However, it can vary, practically up to 0.5 m below the overflow edge of the clear water drain. Thus, the high-performance thickener can work in "storage mode" over a long period of time, ie it can be driven out of the circuit without sludge removal, resulting in a slowly increasing compression of the sludge in the area of the discharge cone of the high-performance thickener and solids contents of up to 30% by this discontinuous removal become.
• - From the distribution box above the multi-chamber reaction basin, clean them the mining water in free fall via one or more inlet nozzles (battery), which in the Work in conjunction with an atomizer based on the water jet pump principle, into the first chamber of the multi-chamber reaction basin, with significant amounts of air by suction for iron and manganese oxidation.
• - The inlet nozzles have a diameter reduction to increase the inlet speed. The number of inlet nozzles, the ratio of the inlet diameter (D ₃ ) and outlet diameter (D ₄ ) of the inlet nozzle and the different fitting lengths (L _e ) of the inlet nozzles are dimensioned so that the incoming raw water flow in the distribution box has a constant water level (H _P ) reached. Fluctuations in the supply volume are compensated for by the different connection lengths (L _e ) of the inlet nozzles in the distribution box, which on the one hand prevents the overflow of the distribution box and on the other hand uses the full suction effect for ventilation even with smaller intake quantities. If individual inlet nozzles become blocked, other inlet nozzles become active with the same mode of action.
• - The multi-chamber reaction tank is divided into at least two chambers to be ventilated. The volume of the respective chamber is determined by the required dwell time of the mining water to be cleaned before overflow into the guide tube, the mean dwell time being 10 to 30 minutes per chamber. The overflows between the chambers in the partition walls are designed and offset so that short-circuit flows are avoided. The chambers are fed separately with precipitant and the pH value is checked by automatically regulated precipitant metering in order to achieve optimum conditions by gradually increasing the pH value to 7.0 to 8.5 in steps of Δ pH from 1.0 to 2.5 for the grain growth of the metal hydroxide gypsum particles and to reduce the proportion of amorphous metal hydroxide in the precipitation sludge. As a result, a higher solid density in the sludge is achieved with a lower recycling rate of the sludge return. By adding barium chloride (BaCl ₂ ) to the multi-chamber reaction tank, radium is co-precipitated from the sulfate-containing medium, which is incorporated into the structure of the metal hydroxide gypsum particles and is thus precipitated.

Embodiment 1

In the following an embodiment of the invention with reference to drawings he purifies. Show it:

Fig. 1 shows a schematic representation of the device with the distribution box, multi-chamber reaction tank and Hochleistungseindicker with guide tube (without Krälwerk)

Fig. 2 distribution box with inlet nozzles and

Fig. 3 inlet nozzle.

The example describes a pilot plant that uses automatic control to control automatic operation how the constant parameter documentation enables an operational solution (rich solution) a uranium mining reorganization company is cleaned.

The pilot plant of FIG. 1, 2 (Fig. 2) of a distribution box with raw water inlet 1, inlet nozzles 3 of different total lengths (Fig. 3) with spray 19, and an overflow 4, a conditioning tank 8, a multi-chamber reaction basin 9 with three chambers 10 and the staggered overflows 11 between the chambers 10 and a high-performance thickener 14 (without caliper) with inlet pipe 12 , guide pipe 13 with constriction just before the outlet, baffle cone 15 , sludge discharge 16 and clear water drain 17 . The sludge return 5 is returned to the first chamber 10 of the multi-chamber reaction tank 9 via the conditioning tank 8 with the addition of the precipitant 6 (lime milk). In each chamber 10 of the multi-chamber reaction basin 9 , precipitant 6 is added and aeration is carried out. Barium chloride 7 is added to the last chamber.

The following cross-sectional areas of the inlet pipe 12 , the guide pipe 13 and the high-performance thickener 14 are realized on the pilot plant:

• - inlet pipe 12 A ₀ = 9 cm ² ,
• - guide tube 13 A ₁ = 87 cm ² ; vertical speed component v ₁ = 1,000 m / h,
• - Guide tube 13 at the constriction A ₂ = 28 cm ² ; vertical speed component v ₂ = 3.060 m / h,
• Guide tube 13 at outlet A ₃ = 66 cm ² ; vertical speed component v ₃ = 1.362 m / h,
• - High performance thickener 14 A ₄ = 620 cm ² ; vertical speed component v ₄ = 0.140 m / h.

The vertical speeds are given relative to the sinking speed in the guide tube 13 . The following parameters are run:

• - pH 2.5 at raw water inlet 1 or 8.5 at clear water outlet 17 ,
• - precipitant 6 calcium hydroxide (as 5 percent lime milk),
• - 3.5 ml barium chloride solution (0.02%) per liter of working solution for radium precipitation,
• - Residence time in the neutralization 60 min.
• - 10 ml flocculant auxiliary solution (0.01 percent) per liter of working solution,
• Return ratio of the sub-discharge of the high-performance thickener 14 to the amount of the operating solution flowing in 1: 1,
• - Area load of the high-performance thickener 14 1.7 m ³ / (m ² h) and
• - Solid composition mainly hydroxides of iron, aluminum and zinc; Sulfates calcium and barium (including radionuclides).

In this pilot plant, the cleaning documented in Table 1 by the analysis data effect achieved.  

Table 1

Analytical data

By gradually increasing the pH in the chamber 10 of the multi-chamber reaction tank 9 from a pH = 2.5 in the raw water inlet 1 , over pH values of 4.0 and 6.0 to 8.5, the solids content in the precipitation sludge increases to over 15 M%.

There is a sharp separation between the floating bed and pure water zones. The turbidity in the clear water outlet 17 is from 20 to 40 turbidity units (TE). The removed sludge is easily dewatered. In a plate filter system, filter surface loads of 0.2 m ³ / (m ² h) can be realized.

By measuring and regulating the sludge level (H _S ) 18 , an operating regime with continuous sludge discharge 16 at a constant sludge level (H _S ) 18 is realized by an automatic measuring and control system.

When the precipitation product of the working solution and the precipitation sludge are immobilized as Binder (BM) cement PZ 45 and the commercial immobilization product Depocrate MF (DHF) used, optionally with admixture of gravel as filler.

The breaking strengths of the immobilized test specimens - after 28 days of curing - are in the Tables 2 and 3 are shown.

Table 2

Breaking strength of the immobilized test specimens from the precipitate of the working solution (BM and gravel proportions relate to the mass of the sludge sample)

Table 3

Breaking strength of the immobilized test specimens from the precipitation sludge (BM and gravel fractions relate to the mass of the sludge sample)

The minimum strength requirements according to DIN 18134 of 0.2 N / mm ² are thus exceeded in all cases. The immobilisates have sufficient buffer capacity to protect the matrix from corrosion by weakly acidic leachate.

The uranium mobilization from crushed material by water is in the range of 10 ^-4 to 10 ^-3 %. The uranium leaching rate in weakly acidic leachate is less than 10 ^-5 g / (cm ² d) for mixtures Nos. 1 and 2 in Table 2 and mixtures Nos. 5 to 8 in Table 3.

Embodiment 2

In a 10 m ³ / h compact water cleaning system, the cleaning of mining water from the lignite mine was tested in a connecting trench between two remaining holes.

The 10 m ³ / h system, which is designed as a container system, consists of two high-performance thickeners 14 with a diameter of D ₂ = 180 cm and a diameter of the guide tube 13 of D ₁ = 60 cm.

The cleaning values achieved when used on site are shown in Table 4.

Table 4

Analysis data of a 10 m ³ lh compact water purification system

An area load of 1.6 m ³ / (m ² h) was achieved.

With this application example, the suitability of the method and the device is also proven for the case when no gypsum precipitation occurs, but only iron hydroxide from falls.  

Reference list

1

Raw water supply

2nd

Distribution box

3rd

Inlet nozzle

4

Overflow of the distribution box

5

Sludge return

6

Precipitant (milk of lime)

7

Barium chloride (BaCl ₂

)

8th

Conditioning tank

9

Multi-chamber reaction basin

10th

chamber

11

Overflow between the chambers

12th

Inlet pipe

13

Guide tube

14

High performance thickener

15

Impact cone

16

Sludge discharge

17th

Clear water drain

18th

Sludge level,

19th

Atomizer
D ₁

Guide tube diameter
D ₂

High performance thickener diameter
D ₃

Inlet diameter inlet nozzle
D ₄

Outlet diameter inlet nozzle
A ₀

, A ₁

, A ₂

, A ₃

, A ₄

Cross sectional area
v ₀

, v ₁

, v ₂

, v ₃

, v ₄

Speed component
v _p

Sinking speed of the particles
H _p

Level in the distribution box
H _S

Mud level
L _e

Integration length of inlet nozzle
L Total length of inlet nozzle
Q _R

Raw water intake quantity

Claims (5)

1.Process for the purification of acidic, iron and sulfate-containing mining waters according to the high density sludge method (HDS method), whereby the mining waters to be cleaned have increased concentrations of uranium up to 50 mg / l, its derivatives, a high sulfate content up to 5 g / l, rock-specific metal ions, in particular iron, and have a low pH between 2 and 4, characterized in that the cleaning of the mining water with regard to uranium, its secondary products and / or the sulfate contamination and metal contamination in a one-step process according to the HDS -Method with the addition of precipitant ( 6 ) and / or barium chloride ( 7 ), the raw water to be cleaned from a distribution box ( 2 ) via one or more inlet nozzles ( 3 ), which in cooperation with an atomizer ( 19 ) after Water jet pump principle work, falls in free fall in the first chamber ( 10 ) of the multi-chamber reaction basin ( 9 ), at the same time in the first chamber ( 10 ) of the recycled sludge return ( 5 ), which was previously mixed in a conditioning tank ( 8 ) with precipitant ( 6 ), the raw water aerated by the free fall and the recycled sludge return ( 5 ) for iron and Manganese oxidation with an average time of 10 to 30 minutes in the chambers ( 10 ) of the multi-chamber reaction tank ( 9 ) before overflow in the guide tube ( 13 ), each chamber ( 10 ) separately with precipitant ( 6 ), with further ventilation of the Raw water, charged and with a view to the pH value by metering the precipitant stepwise, the pH value is increased to 7.0 to 8.5 in steps of Δ pH from 1.0 to 2.5, which by adding barium chloride ( 7 ) into the Multi-chamber reaction basin ( 9 ) the co-precipitation of radium from the raw water to be cleaned takes place, the solid / liquid separation with the addition of flocculation aids in a stable floating bed made of metal hydroxide gypsum particles in a high performance ngs thickener ( 14 ), the major part of the precipitated sludge drawn off at the sludge discharge ( 16 ) of the high-performance thickener ( 14 ) when checking and regulating the sludge level ( 18 ) into the process with renewed, pH-controlled addition of precipitant ( 6 ) and mixture with the raw water is recycled over 10 times and the portion of the inorganic waste sludge drawn off from the process, easily dewatered, is disposed of without intermediate storage. 2. The method according to claim 1, characterized in that with more than 10 times recycling of the precipitate on the sludge discharge ( 16 ) an easily dewatered metal hydroxide gypsum sludge, which firmly includes the precipitated compounds of uranium and its secondary products, with a solids content of over 10 M. % with continuous deduction and up to over 30 M% with dis continuous withdrawal. 3. The method according to claim 1 and 2, characterized in that the resulting inorganic precipitation sludge with conventional Lichen binders immobilized and after curing an immobilizate of high strength and less elutability of the enclosed pollutants under real elution conditions is deposited. 4. Device for cleaning acidic, iron and sulfate-containing mining water, by means of earth or concrete pools, inclined clarifiers or round thickeners with a calving mechanism, characterized in that the inflow of the mining water to be cleaned from a distribution box ( 4 ) above the multi-chamber reaction tank ( 9 ) in free fall Via one or more inlet nozzles ( 3 ) with different lengths, due to different connection lengths (L _e ) of the inlet nozzles ( 3 ) in the distribution box ( 2 ), the diameter of the inlet nozzle ( 3 ) in relation to the inlet diameter (D ₃ ) of the inlet nozzle: outlet diameter (D ₄ ) of the inlet nozzle are equal to 1.5 to 2.5: 1 and at the outlet of each inlet nozzle ( 3 ) an atomizer ( 19 ) with air inlet openings and / or an atomizer grille are fitted in the first chamber ( 10 ) of the multi-chamber reaction basin ( 9 ) according to the water jet pump principle, the multi-chamber reaction basin ( 9 ) from min at least two chambers to be ventilated ( 10 ), the volume of the respective chamber ( 10 ) being determined by the required dwell time of the raw water to be cleaned, and the overflows ( 11 ) between the chambers ( 10 ) in the partition walls are arranged offset that the cross-sectional areas of the inlet tube ( 12 ), the guide tube ( 13 ), which has a constriction shortly before the outlet, and the high-performance thicker ( 14 ) in the ratio of the cross-sectional area of the inlet tube (A ₀ ): cross-sectional area of the guide tube (A ₁ ): cross-sectional area of the guide tube at the constriction (A ₂ ): cross-sectional area of the guide tube at the outlet (A ₃ ): cross-sectional area of the high-performance thickener (A ₄ ) is 0.05 to 0.2: 1: 0.3 to 0.7: 0.5 to 0.9: 5 to 9, the upper sludge level ( 18 ) fluctuating between at least 1.5 m above the outlet edge of the guide tube ( 13 ) and 0.5 m below the overflow edge of the clear water outlet ( 17 ) and the absolute size of the cross-sectional area of the high-performance thickener (A ₄ ) must be adapted to the nominal throughput of the system. 5. The device according to claim 4, characterized in that a constant level of the mining water to be cleaned in the distribution box ( 4 ) by the number of inlet nozzles ( 3 ), the dimensioning of an inlet diameter (D ₃ ) of the inlet nozzle ( 3 ) and the outlet diameter ( D ₄ ) the inlet nozzle ( 3 ) and the different embedding lengths (L _e ) of the inlet nozzles ( 3 ) are regulated.