PROCEDURE AND DEVICE FOR the PRODUCTION FROM MERCURY SULFIDE TO attaching ends the DISPOSAL

The invention concerns a procedure for the production from mercury sulfide to the following disposal, whereby the mercury sulfide results during the mixing process in a mixing apparatus from a mixture of elementary mercury and an addition material from elementary sulfur or a sulfur connection.

Mercury is used due to its special physical characteristics in many technological applications and in industrial production. Here in particular the chlorine alkali electrolysis is to be called for the production from chlorine to. Apart from a multiplicity of positive characteristics are mercury in addition, a poisonous dangerous material, which represent a danger for humans and environment in particular due to its already steam pressure comparatively high at ambient temperature. Numerous accidents and almost irreversible environmental damage in the past help mercury to a doubtful popularity.

Before this background today within many ranges mercury or whole production procedures is substituted, in order to reduce the use of mercury and thus mercury emissions as far as possible. The reduced need leads to a reduction up to the attitude of production of primary mercury on the well-known manufacturing plants. Already for many years in recycling plants secondary mercury from wastes is recovered and offered as alternative to primary mercury at the market. Very large quantities secondary mercury are released in the future with the world-wide conversion of existing chlorine productions from the amalgam procedure to the diaphragm procedure. Permanently it will not be possible to use out these plants released mercury in other environmentalfair applications. Before this background will it necessary to provide for elementary mercury a environmentalfair, final disposal possibility for the order.

A possibility of the transformation of elementary mercury into a stabilized mercury compound exists in the production of mercury sulfide (Zinnober). Mercury sulfide is a stable and/or stabilized connection, which permits a permanent and safe storage of mercury due to its well-known characteristics (innocuously, chemically stably, also under aggressive conditions). In all other respects it is in principle also possible to manufacture mercury sulfide using sulfur connections.

From the US-A-5,034,054 is already a procedure for the production of a stabilized mercury compound for the following disposal well-known. Mercury in form of an amalgam in connection with copper, zinc or nickel is bound as addition material or however as mercury sulfide in connection with sulfur as addition material and disposed of afterwards environmentalfairly. With the well-known procedure the addition material with mercury in a stoichiometric relationship of at least 1:1 and preferentially 3:1 is added. The mixing process is accomplished thereby with ambient temperature and ambient pressure. Is from disadvantage with the well-known procedure that the addition material in strongly over-stoichiometric relation to mercury must be added, in order to ensure a sufficient reaction of mercury to mercury compound. A further disadvantage of the well-known procedure consists of that regarding the strong over-stoichiometric surplus of the addition material, which is added in powder form with the mixture process aerosols, i.e. smallest addition material particles sedimentierende in air can develop.

Task of the available invention is it now to be placed a procedure and a device of the kind initially specified for the order be manufactured with the mercury sulfide in simple and economical way and if possible without environmental impact can.

This task is solved with a first alternative according to invention essentially thereby that mixing mercury and the addition material takes place during the mixing process at a temperature of more than 50°C.

In connection with the invention it was recognized that the strongly over-stoichiometric addition of the addition material is therefore necessary according to the US-A-5,034,054, since the reaction of the sulfur with mercury can take place in each case at the surface in the solid state available sulfur particle. In order to make a complete reaction possible of the sulfur with mercury, a high surplus of the sulfur is necessary with this fixed liquid reaction. The temperature of over 50°C during the mixing process, increased with the available invention, leads as such first of all to that the steam pressure of mercury is continued to increase. Thus a larger part of mercury changes into the vapor phase, when this is at ambient temperature the case. Altogether the reactivity of mercury is increased thereby and the education is improved by mercury sulfide.

Special regarding a complete conversion of the materials used to mercury is of advantage it, if mixing takes place at a temperature above the fusion point of the addition material, preferably at a temperature by means of 150°C and in particular in the range of the boiling point from mercury. The increase of the temperature on the aforementioned values causes the following. First of all the state of aggregation of the addition material of firm changes in liquid. Further the rise in temperature leads to a further increase of the steam pressure of mercury. At the same time also a sulfur steam develops depending upon height of the temperature. Thus different mixing processes find, i.e. related to mercury/sulfur the mixing processes liquid/firmly, liquid/liquid, liquid/gaseously, gaseously/firmly, gaseously/liquid and gaseously/gaseously in the Mischeinrichtung. In this way an optimized conversion of the materials used is reached to mercury sulfide.

With an alternative preferential execution form of the available invention, which is suitable however in particular in connection with the execution form specified before, it is intended that mixing is accomplished in the Mischeinrichtung with negative pressure. Negative pressure designates each pressure below the ambient pressure up to the vacuum. Are sufficient already small suppress from 0,05 bar, what corresponds with an ambient pressure of 1 bar to absolute pressures of 0,95 bar. The execution of the mixing process in the negative pressure causes, how it described before that the boiling point of mercury sinks accordingly and at smaller temperatures a high concentration of mercury in gaseous form in the mixer housing of the Mischeinrichtung is already reached, whereby mercury reacts itself faster with the sulfur for the formation of mercury sulfide.

It is particularly preferential to accomplish the mixing process in a temperature range within the Mischeinrichtung for instance in the range of the boiling point with mercury with simultaneous negative pressure. Thus it can be achieved that entire still elementarily existing mercury is transferred during the mixing process into the gaseous phase and so that an optimal mixture with the sulfur can take place. In all other respects it is meaningful also under safety aspects to accomplish the procedure according to invention with a reduced pressure in a closed mixer since so even at reaching the boiling point the negative pressure no mercury steams adjusted by mercury according to and/or at smaller temperatures worked can to be able to escape. In all other respects the execution of the mixing process in the negative pressure has the advantage for instance with boiling temperature of mercury that during, an unwanted increase in pressure arising if necessary in the Mischeinrichtung the normal print must be only stopped, which leads at the same time to that the boiling point of mercury rises, which leads with the existing temperature level to immediate pressure reduction.

In particular at the time of execution of the procedure according to invention in the temperature range before mentioned and/or in the negative pressure it is possible to add the materials used in the stoichiometric or a small over-stoichiometric relationship. The stoichiometric relationship from elementary sulfur to mercury is with 0,16: 1. With such a relationship an ideal conversion of the materials used is present to mercury sulfide. During not complete conversion the upper limit value lies at 0,5:1 and thus still 100% below the lower limit of the mixing proportion, which is mentioned in the US-A-5,034,054. Preferred the relationship between elementary sulfur and mercury lie between 0,18; 1 to 0,32:1 and in particular between 0,19:1 and 0,23: 1.

With a preferential execution form of the available invention the Mischeinrichtung is rinsed for the achievement of a oxygen-free atmosphere with inert gas, preferably several times. The education can be excluded by the oxygen-free atmosphere obtained thereby from SO2 during the mixing process.

In all other respects it is favorable for the avoidance of any with mixing arising steams or aerosols, if the mixing process is accomplished in a closed, gas densities area of the Mischeinrichtung. As a result of this closed application in the long run an emission freedom in connection with the procedure according to invention arises.

The mixture of the materials used effected in the Mischeinrichtung prefers thereby that either the mixer housing rotates during the mixing process, or however the mixer housing is firmly installed and a sealed mixer wave with a majority is intended by mixer shovels, which rotate within the mixer housing. The invention is not fixed on a certain number of revolutions. In principle is valid, the better the mixing is, the more intensive, i.e. faster, the reaction between mercury and the sulfur will take place.

With attempts, which were accomplished, it was stated that the mixing process is accomplished over a treatment time between 10 minutes and three hours, in particular between 20 minutes and two hours and in particular between 30 minutes and one hour, in order to ensure a complete conversion of the existing materials used to mercury sulfide.

Instead of an intermittent procedure is it in principle also possible, a continuous procedure for the immobilization of mercury by reaction with sulfur to mercury sulfide to be made, whereby a reactor is fed continuously with mercury and the addition material, whereby mercury and the addition material in the reactor are warmed up and transferred into a gaseous condition and whereby the reaction between mercury and the addition material takes place in the gaseous phase.

Device in accordance with a preferably indirectly heatable reactor for the transfer of elementary mercury and an elementary sulfur and/or a mercury compound containing addition material is intended into the gaseous condition for the solution of the task initially specified, whereby the reactor can be fed over an accordingly trained feeding device continuously with mercury and the addition material. With the reactor it can concern a preferably upright standing tubular reactor, which ensures high turnover rates of the gaseous components. In all other respects the indirect heating of the reactor leads to a procedure A KINDLINg.

In connection with the continuous production of mercury sulfide it is further intended that the mercury sulfide available with the reaction in the reactor is exhausted continuously vaporous from the reactor. The operating temperature in the reactor is thereby preferably above the boiling temperature of mercury sulfide and/or above the evaporation temperature, so that the formed mercury sulfide condenses and/or resublimiert not within the reactor. The operating temperature in the reactor should from there preferably above approx. 580° lie, can however be also more highly selected, in order to be able to exclude a condensation and/or a Resublimation surely from mercury sulfide. If the reactor is operated with negative pressure, the operating temperature can be reduced also accordingly.

The enterprise of the reactor at temperatures within the range above the boiling temperature of mercury sulfide leads in all other respects to that the materials used are transferred after the entry into the reactor very fast into the gaseous phase. Thus the necessary retention time in the reactor lets itself reduce accordingly and to accordingly increase the output of mercury sulfide.

The reactor can be fed with a preferably homogenized mixture from liquid mercury and powdered addition material. This makes a process engineering simple continuous filling possible of the reactor with the basic materials. It understands that a feeding device must be planned, which is trained for the continuous filling of the reactor with the homogenized mixture. In principle also a proportioning plant can be intended, whereby mercury and addition material are supplied to the reactor from collecting main containers separately in the desired mixing proportion.

The design of the reactor and the Stofünengeströme should be so selected that the computational retention time of mercury and addition material in the reactor amounts to at least one second until 6 seconds, preferably less than four seconds. Thus a sufficient conversion is guaranteed with the gaseous phase reaction between mercury and the addition material.

Preferably the reactor and also the further mechanisms taken part in the production of mercury sulfide are gas-tight operated during the device according to invention, so that it cannot come with the continuous production of mercury sulfide to escaping mercury sulfide into the environment. Thus a environmentalfair production of mercury sulfide from the materials used is possible.

The reactor can be subjected over a vaccum pump or a vacuum blower with a small negative pressure, in order to meet the working reliability and a withdrawing of mercury sulfide from the reactor to exclude be able. It understands itself that the enterprise under small negative pressure concerns all mechanisms of the device according to invention, which are flowed through by gaseous mercury sulfide.

Further it is intended with the procedure according to invention that the vaporous after mercury sulfide would drive off from the reactor with a liquid or vaporous cooling agent suddenly at least up to reaching a solid state, preferably up to a temperature of less than 50 °C, one cools down and together with the cooling agent of a fixed liquid separation one submits. With the cooling agent it can concern water, whereby for the cooling of the mercury sulfide a Quench and/or a water-operated vacuum pump can be planned. So that it does not come to an inadvertent condensation and/or Resublimation of mercury sulfide before the sudden cooling, a heatable line for the mercury sulfide between the reactor and the Quench and/or the water-operated vacuum pump can be intended. With enterprise of the Quenchs or the water-operated vacuum pump a sufficient pressure gradient adjusts itself to the reactor in the rule enterprise, so that the possibility exists to operate the plant without vaccum pump or vacuum blower with small negative pressure without escaping mercury sulfide must be feared into the environment.

The Quench or the water-operated vacuum pump can be fed with cooled water, which leads to a sudden cooling of the vaporous mercury sulfide, which is supplied in the following together with the water of a fixed liquid partition stage, in order to separate the cooled down mercury sulfide from the cooling agent. The cooling agent can be led in the cycle, which leads to a saving of operating cost.

The fixed liquid separation from firm mercury sulfide and liquid cooling agent can take place via force of gravity separation in a sedimentation basin and/or via centrifugal force separation in a centrifuge. The high density of mercury sulfide of 8,1 g/cm3 makes thereby a simple and economical separation possible of mercury sulfide from Kühlbzw. Washing water. In such a way received firm mercury sulfide can be pressed following the fixed liquid separation and dried if necessary. In this connection a Preßeinrichtung, preferably a Filterpresse, can be intended, whereby the so available filter cake from mercury sulfide in the connection in a vacuum mixer and/or a drying oven can be dried.

Preferentially in all other respects is it, if according to invention the mercury sulfide manufactured in the procedure is exhausted after mixing over, a closed discharge equipment coupled with the Mischeinrichtung. The manufactured mercury sulfide without dust mission can be removed and be filled up by the realization of a closed discharge equipment afterwards dust proof into appropriate containers for the final storage.

With attempts, which were accomplished, it was stated that the mixing process - dependent on the process conditions, i.e. in particular the temperature and the negative pressure put on - should be accomplished over a treatment time between 10 minutes and three hours, in particular between 20 minutes and two hours and in particular between 30 minutes and one hour, in order to achieve a complete conversion of the materials used to mercury sulfide. Can - depending upon size of the Mischeinrichtung per mixing process a load between 10 and 10,000 litres at materials used be supplied.

In all other respects it can present itself to supply the Mischeinrichtung forwards or during the mixing process at least one aggregate for the conditioning of the manufactured mercury sulfide. In particular an aggregate can be used, by which the mercury sulfide receives a granular form.

Preferentially is it further, if the mercury sulfide is exhausted after mixing over, a closed discharge equipment coupled with the Mischeinrichtung. It can be guaranteed by a such closed discharge equipment that also with the withdrawal of the mercury sulfide no emissions arise, so that the entire process can be accomplished in the long run at least essentially emission-free.

Device in accordance with a mixer housing exhibiting Mischeinrichtung is intended for mixing elementary mercury with the addition material in connection with the procedure described before. It is intended with an alternative according to invention that a heating mechanism is assigned to the mixer housing, in order to heat the materials used up in the mixer housing at least over ambient temperature.

With the alternative execution form, which is suitable however in particular in connection with the aforementioned execution form, the Müscheinrichtung is designed as vacuum mixers with a pressure tight mixer housing, whereby a vacuum pumping mechanism is assigned to the mixer housing.

In all other respects the mixer housing favourable-proves a Intertgaszuführung is for the inertization of the mixture area assigned.

Further points the Mischeinrichtung prefers a rotary drive either for the mixer housing, if this is turned, or however for a mixer wave also mixer shovels fastened up in order to ensure an intensive mixing of mercury and the sulfur. In a by way of trial operated plant with mixer wave and to it fastened mixer shovels im übrigen different numbers of revolutions as well as different wall distances of the mixer shovels were tested. It was stated that with rising number of revolutions and reduced wall distance of the mixer shovels an optimization of the response time is to be observed.

A closed discharge equipment for the mercury sulfide is in all other respects assigned to the mixer housing. Over this discharge equipment the mercury sulfide can be exhausted dust free from the mixer.

Further the device according to invention exhibits one the Mischeinrichtung in procedure direction upstream feeding device, by way of which the replacement materials can be supplied. It understands itself that the feeding device represents altogether a closed system, so that any emissions cannot occur here.

One points out expressly that all and range specifications managing specified all concerned intermediate intervals and individual values including any decimal places, lying indicated in the patent claims, within the range, to cover, even if these intermediate intervals and individual values are in detail not indicated.

Fig. 1 points a schematic representation of a device to the production from mercury sulfide to the following disposal. On the basis the design in the following also the procedure according to invention is described. However it is pointed out that the invention is not limited to the represented execution form.

A device 1 is represented for the production of mercury sulfide (HgS) from elementary mercury (Hg) and elementary sulfur (s) for final environmentalfair disposal. The device 1 exhibits a Mischeinrichtung 2 with a mixer housing 3. During the mixing apparatus 1 it concerns available a vacuum mixer in horizontal building method, whereby it is to be pointed out that other designs and arrangements are not less efficient also possible and.

The Mischeinrichtung 2 a feeding device 4. is upstream in the represented remark example exhibits the feeding device 4 three Vorlagebehälte 5, 6, 7. Liquid elementary mercury is in the collecting main container 5, while in the collecting main container 6 powdered elementary sulfur is. In the collecting main container 7, which is fakultativ intended, aggregates are for conditioning, which bedarfsweise can be supplied to the mixer housing 3 together with mercury and the sulfur, bedarfsweise in addition, only during or after the actual mixing process.

Instead of the represented collecting main containers 5, 6, 7 the supply of the materials used can come alternatively also from mobile containers, which are then put on and emptied depending upon filling above the Mischeinrichtung 2.

From the feeding device 4 and/or the respective collecting main container 5, 6 and 7 is promoted if necessary by means of actually well-known of automatic dosing technology the materials used in the desired relationship to the mixer housing 3. For this a in detail not represented conveyer system serves the feeding device 4, which is final outward, so that neither a withdrawal of mercury nor of sulfur particles or however particles of the aggregate supplied if necessary outward can withdraw.

The filling of the Mischeinrichtung 2 takes place thereby in an easily over-stoichiometric relationship of the powdered elementary sulfur to liquid mercury with S: Hg = (32 + 10): 200 = 0,21: 1. With the relationship S: Hg = 32: 200 = 0,16:1 it concerns the stoichiometric relationship. One points out that the procedure can be accomplished in principle in addition, in every other over-stoichiometric relationship with sulfur surplus. However offers specified the before, easily over-stoichiometric dosage an efficient and complete connection of mercury. The dosage as such effected via a separate weighing of the materials used mercury and sulfur as well as the aggregate from the collecting main container 7. the appropriate weighing equipment following the individual collecting main containers, supplied if necessary, are not represented.

After filling the mixer housing 3 with the materials used in the pre-determined dosage the mixer housing 3 is gas-tight locked and flooded over a Intertgaszuführung 8 with inert gas, for example for nitrogen. At the same time an exhaust of the interior is made by a vacuum pumping mechanism 9. The sucked off gas is supplied afterwards to a filter mechanism 10, with which available an activated charcoal filter concerns. Subsequently, the abgereinigte exhaust air from the filter mechanism 10 is exhausted. The inertization of the mixture area within the mixer housing 3 represents available a safety routine, in order to exclude unwanted reactions of the materials used with oxygen. The inertization is however not compellingly necessarily, fundamental can without the Intertisierung be also done.

At the same time with or after the inertization over the vacuum pumping mechanism 9 a negative pressure in the mixture area of the mixer housing 3 is produced. Available a negative pressure is stopped by 0,1 bar with an absolute pressure of 0,9 bar in the mixer housing 3 over the vacuum pumping mechanism 9. Then the mixer drive and thus the mixing process are started. The mixer wave 3a with the mixer shovels 3b fastened to it begins to turn with small number of revolutions. Thereby mixing and a fine dispersion of liquid mercury with the sulfur powder take place after short time. Due to the negative pressure put on and the steam pressure increase of mercury resulting from it a spontaneous reaction of mercury with the sulfur begins.

Parallel to the started mixing process the mixer housing over ambient temperature is warmed up. For this the mixer housing 3 an assigned heating mechanism serves 1. the heating mechanism 1 affects the outside wall of the mixer housing 3. by the outside heating of the mixer housing 3 arises directly an indirect heating of the mixture area as a result of the walls of the mixer housing 3 through and a heat transmission on the materials used in the mixer housing 3. The heating of the mixer housing 3 takes place until in the mixture area the boiling temperature of mercury is reached. Since the procedure is accomplished in the negative pressure, the boiling temperature of mercury is reduced in relation to the boiling temperature with space conditions. With a preferential execution form with small negative pressure the boiling temperature in the mixture area was reached with 320°C. The controlling of the heating takes place as a function of appropriate sensors, which are coupled with the heating mechanism 1.

Depending upon adjusted vacuum and/or absolute pressure in mixer housing the 3 as well as due to the rising temperature now a part of the mercury and the sulfur, which exhibit a fusion point between 112°C to 119°C, goes into the gaseous phase over. Due to the high affinity of mercury and sulfur the developing gaseous phase reacts immediately quantitatively to mercury sulfide. Due to the comparatively high steam pressure of mercury fast mercury steams are formed, which leads first to a better distribution of mercury and reaction at the surfaces of the sulfur particles. With exceeding of the fusion point of sulfur and further heating up increasingly also sulfur steams are then formed, which react immediately under these optimal conditions with mercury steams to mercury sulfide. The combination of the liquid solid reaction with the parallel running gaseous phase reaction leads now within the mixer housing 103 to a very fast and complete conversion of existing mercury to mercury sulfide. The actually existing disadvantage of the bad miscibility of liquid mercury with its high density and surface tension with sulfur powder is compensated with the available procedure by at least partial transfer of mercury in the gaseous phase and the partial transfer of the sulfur in the liquid and the gaseous phase.

In accomplished attempts the complete conversion could be proven in a load, i.e. with a mixing process in the mixer housing of 3, contained mercury by following measurements of the mercury concentration in the atmosphere over the mercury sulfide. In addition samples of the produced mercury sulfide were filled following into gas-tight lockable glass bulbs and the atmosphere by atomic absorption spectrometry (CARRION), adjusting in it, examined itself. No free, i.e. elementary mercury could be proven more with application of this method.

After complete reaction the mercury sulfide is taken over a not represented emptying flap of the mixer housing 3. The emptying is made by a not represented closed discharge equipment, with which it can concern a preferably cooled auger. This does not only make it possible to cool down that mercury sulfide to fill up but this also without dust mission from the mixer directly into dust proof attached container 12 suitable for the final storage.

As was before already implemented, it is by the aggregate in the collecting main container 7 as well as by further, if necessary in further collecting main containers aggregates present possible to condition the manufactured mercury sulfide within the mixer housing. Like that it is easily possible for not making dust consistency by appropriate aggregates, the mercury sulfide in more granular to manufacture in order to make possible thereby also the open handling of the manufactured mercury sulfide.

For the production of mercury sulfide in the procedure described before in a test range treatment times were determined during a complete conversion of mercury between 30 minutes and one hour. The attainable throughput of the device 1 depends in the result on the size of the used Mischeinrichtung 2. When using Mischeinrichtungen with 100 to 10,000 litres daily several tons mercury sulfide can capacity be produced.

Fig. a schematic representation of a device points 2 to the continuous production from mercury sulfide to the following disposal.

In Fig. a device 101 is represented 2 for the production of mercury sulfide (HgS) from elementary mercury (Hg) and elementary sulfur (s) for final environmentalfair disposal. With mercury it preferably concerns secondary mercury. The device 101 exhibits a reactor 102, which is as upright standing tubular reactor trained and indirectly heatable and which as the transfer by elementary mercury and an elementary sulfur and/or a sulfur connection containing addition material is trained into the gaseous condition. It is not in detail represented that the reactor 102 exhibits a feeding device, which makes a continuous filling of the reactor for 102 with mercury and the addition material possible from a collecting main container 103. The collecting main container 103 contains before miscellaneous items and a to a large extent homogenized mixture of sulfur and mercury.

In the reactor 102 those becomes above Siedebzw with an operating temperature. Evaporation temperature of mercury sulfide lies, which transfers continuously the reactor 102 supplied design mixture from mercury and elementary sulfur into the gaseous condition. A gaseous phase reaction continuously running off between the materials used available in the gaseous condition follows, whereby the so available vaporous mercury sulfide is exhausted with a computational retention time of the materials used in the reactor 102 from more as one second until preferably less than four seconds continuously from the reactor 102 and supplied to a Quench 104. An exemplary represented line 105 between the reactor 102 and the Quench 104 is heatable, in order to prevent a condensing and/or Resublimieren of mercury sulfide in the line 105.

With the gaseous phase reaction in the reactor 102 red crystalline mercury sulfide is received. Red mercury sulfide is insolubly, stable and innocuous in water, acids (exception aqua regia) and caustic solutions. Therefore red mercury sulfide for the permanent disposal is suitable.

The Quench 104 is also fed in the cycle led cooling water, so that it comes in the Quench 104 to a sudden cooling of the mercury sulfide into the range of the fixed phase of mercury sulfide. Preferably the mercury sulfide is cooled down on a temperature between 25 °C and 50 °C. Subsequently, in such a way received firm mercury sulfide as well as the cooling water of a fixed liquid partition stage is supplied, whereby in a centrifuge 6 the firm mercury sulfide is separated from the liquid cooling water. The cooling water is led back afterwards to the Quench 104, whereby an inserted cooling of the cooling water can be planned.

Following the fixed liquid separation the mercury sulfide of a Filterpresse 107 is supplied. In such a way produced filter cake can be dried in the connection in detail a not represented drying mechanism and into camp bundle 108 planned for dumping is then filled.

A vaccum pump 109 is in all other respects intended, in order to seize and to an activated charcoal filter 110 supply vaporous mercury sulfide portions. The activated charcoal filter 110 passing gas flow can be led away to it into the environment.

In the result by the available invention a procedure and a device are made available for the production from mercury sulfide to the final environmentalfair disposal, which is characterised by a high efficiency with complete reaction of mercury with high Arbeitsund emission security with at the same time relatively small technical expenditure.

1

Device

2

Mischeinrichtung

3

Mixer housing

3a

Mixer wave

3b

Mixer shovel

4

Feeding device

5

Collecting main container

6

Collecting main container

7

Collecting main container

8

Inert gas supply

9

Vacuum pumping mechanism

10

Filter mechanism

11

Heating mechanism

12

Container

101

Device

102

Reactor

103

Collecting main container

104

Quench

105

Line

106

Centrifuge

107

Filterpresse

108

Camp bundle

109

Vaccum pump

110

Activated charcoal filter