DE2151267A1 - METHOD AND DEVICE FOR THE PRODUCTION OF ACTIVATED CHARCOAL - Google Patents

Description

Method and apparatus for producing activated carbon The invention relates to a method and a device for the continuous reactivation of spent carbonaceous adsorbents or for continuous production of activated carbon from virgin raw material.

In the commercial use of granular carbon adsorbents E.g. for the discoloration of sugar syrup, the adsorbent is replaced by different Impurities, some of which are responsible for the color of the syrup, saturated over time. With a certain one State of saturation the carbon is practically no longer effective and must be replaced by appropriate Facilities are reactivated, provided the repeated use is economical can be realized. Such reactivation must be associated with low costs be and should be done in such a way that a) again a high degree of adsorptive power and b) the lowest possible loss of volume of the carbonaceous adsorbent is present.

These two factors largely determine the profitability the reuse, as the necessary reprocessing of new adsorbents makes additions of adsorbents necessary for each unit of cleaned goods a usable level of activity and the original volume of adsorbents is maintained. An important consideration is that the activity of the carbon is kept at a well-controllable level, so that the volume losses Control the processing, whereby these losses are kept to a minimum an appropriate treatment facility should be reduced.

What is certain is that, under certain circumstances, a process is responsible for it It may be that more adsorbent surfactants are produced than originally entered into the process. This comes about when the adsorbed Organic contaminants break down and form a carbon deposit that is activated in the course of the procedure itself. In other words: the recovery activated adsorption agent can be greater than 100. In general, however, are the impurities adsorbed by the surfactant adsorbents were, either organic or inorganic nature. if it if they are organic, they tend to oxidize and form carbon monoxide or carbon dioxide and water or volatile acids such as e.g.

Acetic acid, i.e. products that are simply activated by the adsorbent can be separated and blown out of the reactor. If it is inorganic Substances, they usually oxidize and form soluble products or water-insoluble products Solids such as oxides, salts or gaseous substances such as sulfur dioxide or carbon dioxide.

When regenerating a used plastic-containing material it is necessary to have substantially all of the pores both large and large to unlock the smaller ones in the entire pore spectrum to get a fully reactivated one To get carbon that does not have slow progressive changes in the Subject to adsorption properties after repeated reactivation. Although the Larger pores play a more important role in discoloration, the finer ones nevertheless important for the removal of low molecular weight impurities, which are often responsible for color development in organic solutions.

By heating alone, a part (often a substantial part) of the adsorbed impurities by volatilization and destructive distillation removed from the deposit. However, such removal is always incomplete and leaves a carbonized deposit on the internal adsorptive surface. In this state, the carbon has a large part of its original state Discoloration power, as the larger pores represent the places of color adsorption, very are effectively open. However, repeated adsorption and heating cycles require a gradual increase in density and a decrease in adsorptive power until the adsorbent becomes very ineffective.

Once this process has progressed over several cycles, the carbonized deposit due to oxidation is very fire-resistant, and it becomes increasingly difficult, if not / possible, to do them without burning some of the original ones Carbon skeletons - even with controlled oxidation - to be removed.

Consequently, for a complete reactivation it is urgently necessary, to ensure that the remaining deposit is carefully removed, and that this is done immediately and completely after each use, to the greatest possible extent Maintain effectiveness in the process.

A process for the production or regeneration of activated carbon, in which finely divided carbon is fed into a combustion chamber e.g. in the French U.S. Patent 1,377,619. In this procedure Carbon fed into hot inert gas and then carbonized and activated. Hence, it is at least a two-step process. The US patent 1 641 053 relates to a method in which all reactants are entered at the same time takes place in a reactor closed on all sides. Likewise, although in British Patent 213 94c describes the carbon particles in a valuable transport reactor forwarded by gases no information about the mixing techniques for the introduction of the carbonaceous material, nor is there any indication of that Reaction conditions before. The Belgian patent specification 720 575 and the corresponding Canadian patent specification 868 328 describes a one-step process, in which a slurry is placed directly in an upward gas stream, where it reactivates within 1 to 5 seconds at a temperature of 7300C to 9550C will -However, this method has no initial mixing-.

U.S. Patent 1,475,502 also includes a simultaneous Mixing the reactants. US Patent 3,298,928 describes Carbonization conditions in a carbonization reaction, but does not contain any Information regarding the activation of the carbon and does not apply in any case lower temperatures; this is typical of the prior art where omitted will record the critical conditions necessary to activate the carbon.

Other patents describe the various aspects carbonation such as U.S. Patents 1,774,341; 2,166,225; 2,933,454 and British patent specification 638 492. None of the patents cited are deficient a description of the fully operational process. Many known procedures also deal with the derivation of theoretical processes, however, has practice demonstrated that it is difficult to find a really quick and effective procedure to develop.

In the process for production or regeneration according to the invention The carbonaceous material is first of all finely divided by activated carbon Form with a moisture content of less than 7> weight percent in a Entering the loading zone, where it mixes with an oxidizing gas, and then the mixture into a low pressure, high velocity zone of the combustion gases passed from a combustion chamber and from there into a reaction zone with at least 9300C, in which there is an excess of oxygen and in which the carbon particles carried by the gases and passed through the zone within 1 to 5 seconds will.

The peculiarity of the invention consists in the special process, to mix the carbonaceous material with the oxidizing gases first and then the suspended carbon to the combustion gases that come from a combustion chamber, to mix in, this mixing in a low pressure, high velocity area prior to entering the reaction zone takes place in which there is a critical lower temperature and reaction time.

There is a real demand for a method and an apparatus to reactivate powdery carbonaceous adsorbents which have much lower investment costs for equipment and maintenance costs than is possible with conventional methods in the field.

In the method according to the invention, the maintenance causes of the finely divided material when it is through the activation zone is conducted in a state of suspension, a practically complete penetration each particle of the raw material with the gas phase of the reactor combustion products. The finely divided state of the raw material allows the process to be controlled so that it can be regulated more evenly than was previously possible. The process also works extremely quickly, with the yield of active carbon compared to known processes is significantly higher.

These advantages can practically only be achieved if all particles of the carbonaceous material in close contact with the reaction gases during remain throughout the treatment, so that the heat and the supplied gases are uniform can penetrate and activate the material.

Another advantage of the present invention is one new device which is suitable for activating finely divided dry or moist carbon-containing »solids» is.

Another advantage of the invention is the ability of the process To regenerate carbon particles in a dusty state. With the concerned Processes are all the better results in terms of activation obtained, the smaller and more uniform the particles are.

To effectively remove the carbonized deposit, keeping the original Activated carbon skeleton is preserved and this consequently maintains its original hardness, it is of paramount importance that Oxidation ability of the gases to burn off the non-volatile deposit from the active surface of the carbons zll control. The ability to oxidize is through influences the following factors: a) by the gas composition and b) by the temperature. In terms of temperature, there is considerable leeway by controlling the temperature Gas composition possible, however, if the temperature drops below 705 ° C, an ever decreasing control of the oxidizing ability is possible, if the speed is kept at a practical level. Obviously the The upper limit of the temperature range can be exothermic as well as endothermic Oxidation reactions take place at remarkable rates and one careful consideration of the gas composition can be maintained in order to eir high levels of precision and control to effect the rate of decarbonization. The temperature should therefore be at least 0) () ° C and preferably between 930 ° C and 985 ° C.

It was also found that when air is an oxidizing gas is used, the sensitivity of the process is remarkable through addition small to medium proportions of steam can be improved. The activation with steam, the entire interior of the particle is uniform. For example starts the actual activation effect of air at a relatively low one Temperature of approx. 430 ° C, but when steam is added the @@@ i @ ierun @ at approx 815 ° C begins. Hence @ the mixture of two gases produces the most uniform and most active product.

When using the method described, the materials that are to be carbonized or reactivated, in a floating state, and are in this state through the combustion products of the reactor filling and through the volatilized organic materials as well as by those during activation resulting moisture.

The treatment time is made accurate by intervening in the speed and the volume of the reaction products itnI the temperature due to the characteristic achieved the combustion is controlled. In particular, the raw material is in the lower end a vertical reaction chamber of previously calculated size and length introduced and the activation gases are in a stream simultaneously with the material filling such speed and strength entered that the material parity in the itself moving gas atmosphere for a period of time sufficient to activate being held.

Thanks to the close contact between the material and the activation gases and thanks to the state of distribution of the material, that is necessary for activation Time very short. In particular, it should be noted that while the solid material and the various gases are entered continuously at the lower part of the arrangement, the activated material is continuously withdrawn from the top of the reactor.

Using the preferred method and related procedures Device, the wet or dry carbonaceous solids are mechanically in a @eschlekungskammer, where steam and / or air the solids over a short distance into a Venturi tube that brings the combustion chamber to the Reactor connects. The high speed and turbulence of the combustion products plus the immediate expansion and ignition of the supplied steam and any more humid or more volatile Shares in the carbonaceous solids leads to an almost spontaneous heat transfer and mixing of the combustion gases with the solid reactant filling. The temperature of the combustion products is caused by the heating of the raw material feed, by the moisture of the feed and by the steam and / or by any air that is in the charge Controlled amounts can be introduced at the desired operating temperature degraded. The suspended solids are directed to the digging of the reactor, where the moisture is removed from them and where the adsorbed organic components transferred into the gaseous phase and / or onto the surface of the carbonaceous Solids are led. The controlled percentage of oxygen in the gas phase, which surrounds the carbon particles, oxidizes the more available, essential ones Volatile substances that generate heat waste and thus continues the required supply of heat down to the reactor. The oxygen also improves the capacity of the reactor as a result its higher capacity, compared to the burning up of the adsorbed organic substances that of the slower steam carbon reaction. From the moisture of the Feeding or controlled addition of steam appears to be effective of oxygen during the phase of the destruction of volatile substances. The steam plays a major role in achieving an en @ valid level of activity especially in the area of the small pore size, as measured by the iodine number test became. If oxygen is used alone as the oxylating gas for reactivation, thus an excellent large pore development is obtained in a relatively short time Duration of action, however, the yield and the iodine value are lower than in combination with steam. Of course, depending on the gas concentration, the reactants occur and the temperature, the oxygen-carbon, the steam-carbon, and the Carbon dioxide-carbon reaction at different points in the reactor at the same time on. It was found that the oxygen-carbon reaction primarily is present in the lower half of the reactor. This can be complete from the almost spontaneous Combustion of oxygen in the gas phase and from the high heat loss in this Section to be closed. The steam-carbon reaction appears everywhere there to be present where the vapor concentration and temperature are favorable. The height Speed in the throat of the venturi prevents it from accumulating on the wall the nozzle throat or in the combustion chamber adhering solids. Upon entry of the material in the reactor, the solid phase is essentially dry and free of and above any sticky volatiles suspended in the gas phase, which prevents deposits on the reactor will. After passing through the reactor, the activated or regenerated carbon can by means of cyclone separators and bag filtering or by wet cleaning and pressure filtering to be collected.

Consequently, if the yield is high, a higher quality one becomes activated Carbon within a short treatment time using a constructive very simply designed facility with no moving parts.

An embodiment of the invention is illustrated below with reference to the drawing described. 1 shows a partially broken front view of an exemplary device to carry out the procedure; 2 is an enlarged corrugated view of the lower one it the reactor chamber for the activation device; Fig. 3 a schematic overall view of the activation device with a device for Recovery of the activated carbon.

Fig. 1 shows more or less schematically the device for generating activated carbon from a virgin raw material or for regeneration of used, previously activated carbon. The device is for treatment of raw material in a finely cut or powdery state. Demand after such a device and a corresponding method was in particular with the increasing application of activated carbonaceous materials as a means of eliminating water pollution acute. Not just public institutions use more and more activated carbon in their water purification projects, but also runoff water from industrial sources is using activated carbon as an anti-pollution agent treated. As this and other new areas of application the demand for large Generated amounts of dusty activated carbon is a cheap, practical and effective method for the production of activated carbon and for Regeneration of used activated carbon is a real necessity.

The main part of the drawing shows an elongated transport reactor which is generally arranged vertically and denoted by the reference number 10 is. The feed of raw material in a finely divided state into the reaction chamber of the reactor is carried out by a funnel-shaped element 11, which is on the side of the Reactor is attached. The raw material is fed into the reaction chamber through any Facilities depending on the type of raw material. As the raw material either is in a moist or dry powdery form, the charging arrangement from the hopper 11 to the transport reactor 10 is corresponding to interpret. For a relatively moist, still in a solid state Material with surface moisture could be a mechanical loader be used.

In particular, for spent grain syrup carbon the material then considered moist when the moisture content is in the range of 60 to 75 Percent by weight.

For moist material, i.e. material that contains less than 60% water, is a forceful injection of the raw material into the reaction chamber of the reactor feasible. The latter type of raw material feed can be carried out by means of a centrifugal fan or other powerful air pressure equipment.

At the extreme end of the screw conveyor 12 is a drive roller 13 attached, which wlrd driven by a drive belt 14 from the engine 5. The motor is expediently operated with a variable speed and is controlled by a resistance control controlled to a specific control of the feed rate in an intermediate chamber of the reactor to be able to make. It is * indescribable, the oxidizing gas, which contains either steam and / or air, in or essentially in the reactor close to the area where raw material loading takes place. This can in different ways, only one of which is shown. The drawing shows a tubular line element 15, which is immediately below the screw conveyor 12 is attached and opens into the small loading chamber 17, where the steam is mixed with the carbonaceous filling 16, the loading chamber 17 is preferably above the reactor combustion chamber 18 in the area of a taper 19, a venturi-like Arrangement of the reactor arranged, whereby the mutual effect of the mixed turbulent combustion gases, of the carbonaceous raw material and the superheated steam are favorably influenced will. This particular arrangement produces a more than satisfactory simultaneous Mixing of the different products and therefore contributes to the extremely fast reaction and to achieve a high yield of activated carbon products.

The operating sequence begins as soon as the steam and / or air is released the line 15 through the solid filling 18 in the finely divided state the charging chamber 17 leads into the taper 19 of the Venturi tube. At this Place the supplied steam, the existing moisture and the volatile substances on or in the carbonaceous raw material with the at high Temperature products of combustion from the combustion chamber 18. The Combustion chamber 18 is filled with a fuel e.g.

Natural gas or propane gas through a line 21 with an excess of air to generate the high combustion temperature, The combustion chamber consists of an outer shell made of ceramic insulation fiber 31.

Inside the ceramic insulation laser 31 and adhering to it is another ring made of an insulating castable material 32, as well as a a relatively narrow layer of ceramic cladding and finally a high temperature resistance plastic refractory inner wall 33.

This combination of insulating and heat-resistant layers causes the combustion chamber to operate at temperatures up to 1,760C can. The temperature is measured by a thermocouple 34.

The taper 19 of the Venturi tube has such a size that A high speed of the gaseous products is ensured, which penetration of the carbonaceous solids into the combustion chamber 18 and structure of solid materials on the wall of the Venturi tube. Also experienced the gaseous phases an optimal and uniform heat transfer and a almost simultaneous mixing.

The suspended solid phase is released from the gaseous reactants and products carried and passed through the reactor, with the necessary residence time for volatilization, thermal splitting and the necessary reaction between the various products available. The lower part of the reactor, as Designated zone 1, produces drying and initial volatilization of the Raw material In Zone II an exothermic reaction occurs, with the main oxidation of organic volatiles and carbon deposits in the presence of Oxygen takes place. Finally, the steam activation takes place in Zone IIIXwo Water and carbon combine and carbon monoxide, carbon dioxide and form hydrogen in an endothermic reaction. The ones in the drawing in general noted zone divisions, characterized by the thermocouple units 34 - 35, 35 - 36> and 36 - 37 need not be viewed as definitive or limiting to become. It is not possible to specify the exact location where the various Reactions take place, but theoretical calculations have shown that the various reactions essentially take place where they are shown. The processes described above wi '] eii on the raw material to depending on the type of raw material used, either a highly active carbonaceous one Generate solid or a reactivation of spent activated carbons.

The products of combustion and the activated carbon pass through the upper one Part of the reactor which consists of a tube 22 made of stainless steel, which is from a high temperature resistant insulation 23 is surrounded. This construction ensures adiabatic conditions on the outside of the reactor and ensures that a uniform high temperature is maintained over the entire length of the reactor. The floating ones Solids pass through a branch pipe 25 into an appropriate line 27 to the recovery device. An overpressure discharge opening 26 at the top of the Reactor is used to protect against the risk of explosion.

As previously noted, it can be used as a recovery facility of the now activated carbonaceous solid is any of the various Species are used, however, the experimental investigations were made with the help of a water sprinkling unit, which is a preferred method. Fig. 3 shows more or less schematically the recovery device from two eductor washers 40, 41, which are in series with the discharged from each eductor Are switched well, with the material flowing into a tank 42. Pumps from tank 42 a pump 43 returns the low-viscosity paste through the eductors 4Q, 41 and generates it the necessary pressure to distribute the pulp to the five pressure filters 45 to 9. Each individual eductor heater acts on the gaseous reactor products to the Removal of the activated carbon by moving the gaseous mixture into the area a high pressure water flow is conducted. The activated carbon is subsequently Spread with the washing water and then by the washing water through the pressure filter 45 bis 49 deposited.

When the final product leaves the filters it becomes the activated carbon product collected for the purpose of further use.

If using another device, the product in the dry Condition, it can be packed for immediate dispatch.

A lavor test facility was used to carry out investigations to determine the optimal operating conditions and to develop the device produced to carry out the various process steps.

The test facility was constructed according to the outlines of the unit shown in Fig. 2 is constructed, and contains the following equipment. First was a pin roller processor from Bethlehem Corporation for preconditioning of the spent carbon samples used prior to activation. This existed from a horizontal cylindrical container of 305 mm in diameter and 914 mm Length with a steam heated rotating element and a steam surrounded clam. In this container, the carbon samples were prepared so that the moisture content of the raw material was not more than 75% by weight or less to the material charge to lighten. The loading unit was made from a stainless steel hopper manufactured, the dimensions of which were 355.6 x 355.6 x 660.4 mm, which is the Width of the two side walls and the depth of the entire unit acted. The lower Part of the funnel was then tapered in one direction so that this on a 25.4 mm screw conveyor element fit that on the floor of the funnel and extended into the housing of the reactor. the The screw was driven by a zero to maximum value variable speed motor, around the material loading rate and the delivery of the carbon sample into the loading chamber to control near the taper of the venturi tube of the reactor combustion chamber.

The dimensions of the furnace or combustion chamber part of the reactor were as shown in Figure 2, 6C9.6 mm in diameter and 457.2 mm in depth. The furnace w @ it a conch made from a tube with a welded flat steel bottom plate and a cover plate @ was made of @ ostfrei @ steel. The inner core of the verb @ ennobling chamber was made of a high-temperature-resistant plastic insulation in the form of a venturi tube The combustion chamber was manufactured with an opening diameter of 19.05 mm then set up to fit on appropriate burners, and it came with connected to the operation of the reactor column.

The insulation around the combustion chamber was made of high temperature resistant castable and compact fiber insulation material, while the torch is a North American XS 4424-C high temperature nozzle mixed gas burner which was arranged in a perpendicular position to the furnace floor.

As for the reactor column, a 1828 mm long tube was made of stainless steel Steel No. 510 with a diameter of 152.4 mm is connected to the top of the furnace in a flange-like manner and fitted with a stainless steel tee and a pressure release port.

The T-piece was necessary to provide an outlet for the combustion gases and as a product to get while the explosion protection opening was added for security reasons. Electric heating elements controlled by resistance were controlled on the outer surface of the stainless steel column for the purpose of compensating for any heat losses through the wall of the reactor and to maintain an approximately constant temperature along the whole Column length arranged. The recovery system comprised a water sprinkler unit, which had a 101 per mm stainless steel tube inclined at 450, which connected to two venturi scrubbers from Schutle and Koerting connected in series was. The first unit was 101.6mm and the second by a 76.2 mm unit and both put the wet product in a tank of 132 Liter capacity of stainless steel. The exhaust gases were through a Line led to the outside with an exhaust fan. That used for the scrubbers Water was taken from the general water supply line and continuously collected in a separate 220 liter tank, from which the water is sent to the scrubber by means of a 1.014 PS Moyno pump with a maximum output of 5154 liters / hour. pumped became.

The recovered pulp product was then passed through a 2.028 PS 88 liters / min. Centrifuge pump for six cup pressure filters with a diameter of 406.4 mm pressed.

The propane gas used as the fuel was measured with a meter from the Rockwell Manufacturing Company, which is measured with a limiting North American throttle valve, and on the burner for that The correct air gas ratio ensured.

The combustion air was blown by means of a fan from North American, No. 2 300, at a pressure of 0.7 KF cm2 from a single-stage compressor, which was directly coupled to a 0.26 hp engine.

The steam for the reactor was 2.1 Kp cm2 by means of a device supplied by Fischer and Porter and passed through a 6.35 mm pipe that was attached below the housing of the screw conveyor. He was in the cremation chamber entered with the charge of spent carbon.

A number of experiments were carried out with the apparatus described above carried out on the operation of the reactor in a temperature range, wherein studied the results obtained when the feed rate of consumed Carbon and steam, and the concentration of oxygen in the products of combustion of the burner can be varied. At the carbon consumed X that in these studies was used, it was a commercial grain syrup carbon, which originally had a Nuchar CEE grade with an average molasses value of 160 and an average iodine number of 92 to 96 be The consumed carbon possessed one mean molasses value of 50 and a mean iodine number below 50.

The results of these tests are tabulated below Form reproduced.

Example 1: In this experiment a commercial one was used Corn syrup charcoal is used to make the reactivation process more effective to be determined at different temperatures. The occupancy rate was constant 1.294 kg / h (dry) with a steam supply of 1.453 kg / h. The different Temperature levels were achieved by the fire power of the gas and the amount of oxygen in the excess air that passed through the burner became. The oxygen added to the temperature due to the heat drop came from from the oxidation of the volatile substances excreted from the spent carbon became.

Example 1 Temp. Oxygen + MW JW Comment approx kg / h Experiment 1 702 0.37 67 57.8 zuriden-2 756 0.504 93 80.9 standing Regene-3 812 0.515 100 81.0 ration at 980 ° C 4 4 869 0.534 104 82.0 5 5 930 0.635 129 84.5 "6 980 0.715 173 87.7 + calculated oxygen flow rate in the combustion products of the burner.

The results indicate that with increasing temperature and increasing oxygen supply, the molasses value (MW) and the iodine value (JW) rise, until a temperature of 980 ° C has been reached. From then on the values were satisfactory that corresponded to those of the original activated carbon.

Example II: In this experiment, other samples were made from commercial used corn syrup activated, but the steam supply was 2.9 kg / h increased for all experiments, with the same temperatures as in Example I. The spent carbon feed containing about 10% moisture was 1.17 kg / h (dry) with an oxygen flow rate in the combustion products of the burner, which varied between 0.75 and 1.25 kg / h. The oxygen flow rate generally increased with temperature when the burner output was reached a higher temperature level was raised. The measurements were made accordingly carried out the abovementioned Example I and gave the following results.

Example II Temp. Oxygen + MW JW ° C kg / h Experiment 1 702 0.745 91 77.0 "2 756 0.73 113 83.9 3 812 0.656 153 85.6 4 869 0.) 164 89.3" 930 1.255 219 91.5 6 6 980 1.2 198 + calculated flow rate of oxygen in the combustion products of the burner.

This experiment shows the improved operation of the device, if this is operated at higher steam and S @ uers @@ ff rates than in Belspiel I the case @ar.

Again the operating temperature was at the satisfactory MW and JW values were obtained in the temperature range above 9300C.

Example III: In this experiment, commercial, spent grain syrup activated carbon was used investigated at much higher feed rates, the flow rate of the Oxygen in the combustion products of the burner was relatively constant, however increasing amounts of steam per unit of time have been entered. The temperature was held at 9800c.

Example III Charge amount of oxygen + steam MW Jw (dry) kg / h kg / h trial 1 2.56 1.18 2.9 160 91.1 trial 2 2.78 o.88 1.45 145 89.0 trial 3 2.65 1.17 0 123 84.9 + calculated flow rate of oxygen in the Combustion products of the burner.

The experiment shows that the feed rate from consumed carbon over the level after experiments 1 and 2 for the constant reactor volume of 34 000 cm3 could be increased if the minimum steam flow rate per Unit of time equals the rate of charge of the consumed carbon.

Example IV: In this example, commercial []] spent core syrup activated carbon was used regenerated at a charging rate of 3.4 krn "for two hours and 28 minutes. the Steam flow rate was 4.1 kg / h and that of oxygen in the combustion products of the burner 1.8 kg / h. The temperature was at 9800C kept in the reactor and the humidity in the carbon consumed was average 6%. The average carbon content of the carbon consumed was 64.4k (dry).

This value was obtained using a volatile component analysis test behave by placing a sample before and after heating it to 9800C in an inert atmosphere was weighed. The fixed value for the carbon content thus obtained was a measure for the original activated carbon in the spent carbon samples. With knowledge this value and the physical yield of carbon consumed by Measurement of the time input and output quantity into or out of the reactor the percentage recovery of original carbon could be calculated.

Input output charge quantity 3, 25 kg / h production quantity 1.91 kg / h (dry) steam 4.08 kg / h MW 212 O2 in the combustion product 1.8 kg / h JW 92.9 of the burner% solid coal content 64.4%% yield 1.91 = 58.8% of consumed 3.25 Carbon Consumed in Charge of Carbon Moisture Content of the 6%% yield of 58.8% carbon consumed = 91.8% of the original 64.4 Activated carbon reactor volume 34,000 cm3 residence time 1.5 sec.

Reactor temperature 980 ° C constant Purpose of the example IV was the effectiveness of the facility in activating a higher temporal Charge than in the previous examples with the same reactor volume to demonstrate, with a satisfactory activity and yield. the The results obtained show that this is possible and indicate that a consumed Activated carbon material at a feed rate of at least 2.72 kg / h per 28 317 cubic centimeter reactor volume could be reactivated provided the steam flow rate in the reactor corresponds to at least the charge amount of consumed carbon.

Of course, sufficient oxygen must be available for this the organic components that form when the feed is used up Carbon mixes with the products of combustion to oxidize immediately. The very good yield of original active carbon, which can be obtained by measuring the ratio from the percentage of carbon consumed to the percentage of carbon in the feed was 91.8 [beta].

This result was used to ensure measurements over a larger Number of measurements reproduced.

The measurements regarding the iodine numbers and molasses values were carried out, to get a quick and accurate overview of the activation process. Every this test method is common in the industry and can therefore be easily referred to the type of information that is possible with consumers of activated carbon.

The MW determination experiments were carried out by measuring the molasses value of the carbon subjected to the test with the molasses value of a reference carbon compared which serves as a standard measure. The iodine value shows that The percentage of iodine adsorbed by the carbon samples. He is a measure of the total internal surface area that is present in the product. Increasing Iodine values therefore indicate a proportional increase in fine-pored volumes and hence the presence of a desired level of oxidation.

The experiments also show that steam in the process only occurs under such Conditions was necessary in which raw material reactivated in the extremely dry state should be. If the raw material was moist, steam was generated by itself the water in the material. The results also confirm earlier theoretical considerations, which indicated that the optimal operating conditions for regeneration then present when the water content is in liquid or vapor phase that corresponded to the amount of dry material charged.

The experiments mentioned above and others not shown were correct focus on the regeneration of used grain sugar and grain syrup carbons, however, the experience gained in this way allows the process to be carried out in the same way Use of spent carbon in powder form from other areas of application appear usable, e.g.

spent carbon from cane sugar or any other Carbons containing organic materials.

In addition, the described method and the device for Regeneration with a very high yield can be applied to carbon in the form of dust, which comes from the tertiary treatment of runoff water or activated to replace it Sludge is used for the secondary treatment of runoff water. The described new method and device could also be used to regenerate dusty carbon, which is used to produce organic Remove contaminants from chemicals and pharmaceuticals or other media.

The reactor according to the present invention also allows regeneration of other new types of pulverized carbon to make it practical.

E.g. carbon in powder form could be made from coal or other carbons with a particle size small enough for transport regeneration, however larger than the present powdery carbons, regenerated more easily and be recovered as the selected particle size makes filtration because of the greater density and filtering ability improved. In addition, the transport regeneration with a simultaneous reduction in carbon consumption, the use of higher of active carbons for processing appear economical, thereby reducing the cleaning operations be optimized. After all, it likes because of its low cost and high yield the transport regeneration be feasible that acid-washed other special Carbons are used for processing.

As a further example to demonstrate the device described and the methods for activating virgin raw material have become different Experiments carried out on solids containing colylenes from charcoal with the aim of> to improve or develop its activity.

Example V Test conditions: reactor temperature 9800 ° C., steam 7.25 kg / h propane 8.31 SCFH with 2.2% oxygen in the combustion products Results: Charge amount MPW of charcoal (kg) of charge Experiment 1 4.36 22 Experiment 2 6.42 20.8 Trial 3 6.8 20.8 Production amount MPW Yield kg / h of the product % Trial 1 3.3 17 76 Trial 2 5.1 17 79.4 Trial 3 5.24 17 77.0 Example V illustrates the effectiveness of the transport reactor system to improve or develop the Activity of a carbonaceous solid such as e.g.

Charcoal. The modified P @ enol value is used as a measure of the activity (MPW), which is an activity test used for measurement activated carbon is used to treat drinking water. The modified one P @ enol value represents the ratio of the amount of carbon in parts per million, which is required to a phenol concentration of 200% o to 20 Reduce xo. The American Water Woiks Association uses the phenol adsorption test as one of the test methods for measuring the adsorption capacity of activated carbon for Treatment of drinking water.

In the example above, charcoal was made from a bark wood burning stove came through the reactor system at three levels of feed with one Steam feed of 7.25 kg / h passed. The incineration system below the loading point burned 245,000 normal cubic centimeters of propane with 2.2% oxygen in the combustion products per hour. The modified phenol value of the product was found in all three tests significantly above that of the feed and was better than usual for activated carbon for drinking water treatment is required. In the third attempt, the transport reactor system proved to be able to produce a carbon with a good phenolic value at a high feed rate of 5.66 lrg / h per 28 317 cm3 reactor volume under a production volume of 4.35 to generate kg / h per said reactor volume.

The average yield for the three runs was 77. The Uniformity of the phenol value of the product indicates the high feed rate in the third attempt in no way represented the maximum possible loading dimension3. The reactor temperature was kept at 980 ° C. and considered more favorable than lower Temperatures, because at this temperature a better reaction rate for the steam carbon reactin is present.

The example described above describes conditions that can be used Provide activated carbon, but these conditions are by no means exemplary optimal.

It may also be possible to use the transport reactor for treatment dusty carbon in a cleaning and regeneration cycle at substantially lower cost than required for granular carbon to apply. In this case there would be mixing, filtration, washing and carbon regeneration be done more economically in a continuous process.

It also causes the possibility of being regenerated at low cost To obtain powdery carbon, which is cheaper than granular carbon is that other areas of application are possible for this, which so far not considered became.

For example, it has been proposed to use activated charcoal to prevent deposits to use residues from pesticides in animals, especially dairy cattle. Tests have shown that the residues of organic pesticides in dairy cattle can be reduced considerably if a carbon slurry is used Feed is added.

This can be done by adding grains of activated charcoal to either cattle feed The activated carbon is added by the farmer or the feed manufacturer then adsorbs the lance protection agent and continues the build-up of organic matter in the carcass to a minimum.

Claims (10)

Claims 1. - Process for the production or regeneration of active in the finely divided carbonaceous material in a reaction chamber along with an oxidizing gas and with products of combustion for a period of 1 to 5 seconds, by noting that the carbon-containing Material with a moisture content of less than 75 percent by weight in a Feed zone is passed, where it mixes with an oxidizing gas and the mixture then into a low pressure, high velocity zone of gases of the combustion product which come from a separate combustion chamber, and that the mixture is passed into a reaction zone with at least 930 ° C., with an excess of Oxygen is present and wherein the carbon particles are carried by the gases and through the zone within 1 to 5 seconds. be transported. 2. The method according to claim 1, characterized in that g e k e n n -z e i c h n e t that the direction of flow is vertically upwards. 3. The method according to any one of claims 1 and 2, characterized g e k e n n indicates that the carbonaceous material is preconditioned to reduce the moisture content to 75% or less. 4. The method according to any one of claims 1, 2 or 3, dadurchi e k e Note that the oxidizing gas is oxygen. 5. The method according to any one of claims 1 to 3, characterized in that g e k e n n indicates that steam is present in the oxidizing gases in the feed zone is. 6. The method according to claim 5, characterized in that g e k e n n -z e i c h n e t that the temporal loading amount of carbonaceous material and the temporal Amount of supplied steam are essentially the same. 7. The method according to claim 6, characterized in that g e k e n n -z e i c h n e t that oxygen is supplied with essentially the same amount of time as the steam will. 8. TransportreM tor for performing the method according to claim 1, in that it has a combustion chamber, which are connected to a reaction zone by a venturi-like section and contains a loading chamber that is connected to the venturi-like section is in communication, the chamber with a feed for the carbonaceous Material and an independent inlet for the oxidizing gas is provided. 9. Reactor according to claim 8, characterized in that g e k e n n -z e i c h n e t, that the reaction vessel is vertical with the combustion chamber at the bottom End is located. 10. Reactor according to claim 8 or 9, characterized in that g e -k e n n z e i c h n e t that the outlet of the reaction zone to a liquid purifier leads.