GB2038869A

GB2038869A - Process and Apparatus for the Production of Activated Carbon or Coke from a Moist Organic Substance

Info

Publication number: GB2038869A
Application number: GB7940897A
Authority: GB
Original assignee: Outokumpu Oyj
Current assignee: Outokumpu Oyj
Priority date: 1978-11-13
Filing date: 1979-11-27
Publication date: 1980-07-30
Also published as: GB2038869B

Abstract

Moist organic substance (eg furfural residue) is mixed with hot flue gas to dry it, then coked by reduction- burning of the volatile constituents thereof with an oxygen-bearing gas, the coked substance is separated from the gas, or activated by mixing with the hot, moist gas from the coking operation, without separate addition of water vapour, and the activated carbon is separated from the gas, the drying and coking with or without activation, being performed by co-current passage of the organic substance and gas in a continuous zone. Figure 1 shows a cylindrical furnace 3 for carrying out this process. Drying zone 6 equipped with mixing device 5, coking zone 7 into which oxygen-bearing gas is fed via nozzles 8, and optionally activation zone 9 provided with mixing device 5' are arranged continuously. <IMAGE>

Description

SPECIFICATION Process and Apparatus for the Production of Activated Carbon or Coke from a Moist Organic Substance The present invention relates to a process for the production of activated carbon or coke from a moist organic substance, and it relates in particular to a process in which a moist organic substance is first mixed with hot flue gases in a drying zone, whereafter the dried organic substance and an oxygen-bearing gas are directed into the coking zone for a reduction burning of the volatile constituents of the organic substance, then the coked final product is removed from the gas, or the product emerging from the coking zone is directed into the activation zone, where it is mixed with hot, moist gases, and finally the gases are separated from the activated carbon. A further objective of the invention is to provide a cylinder furnace for carrying out the above process.

In connection with the mechanical processing of wood, a great deal of moist residues are produced. Attempts have been made to exploit these residues by burning them. However, the high moisture content in the residue lowers the amount of thermal energy obtained from it. Milled peat used for fuel, even air dried, contains a large amount of water. Also, in furfural production a furfural residue is produced which is rather finely divided and moist (moisture content approx. 40 50% by weight). This residue contains only some ash and a large amount of carbon and volatiles. It can also be destroyed by burning.

The benefit derived from the burning of the above organic, finely-divided substances, which contain large amounts of water, carbon and combustible volatiles, is decreased by their high moisture content. Furthermore, the burning of such substances by means of conventional combustion apparatuses is inconvenient.

In attempts at using the above organic substances in, for example, the production of activated carbon, they are in general at least partly dried, whereafter they are usually first charred and then activated using water vapor. The investment and operating costs of such previously known production processes for activated carbon are, however, considerably high, owing to the several separate treatment stages and the high energy requirement, especially when using superheated water vapor for the activation. When block peat is used as the raw material for activated carbon and when the water vapor activation is carried out in a cylinder furnace, a long reaction period is necessary and the mechanical strength of the product is low. The activated carbon thus produced is not suitable where a high mechanical strength is required of the carbon.

German Patent Application 2,606,368 discloses an apparatus in which the coking and the activation are performed in the same rotating furnace; however, in this furnace the coking zone and the activation zone have been separated by means of a partition. In this apparatus the coked substance is cooled with water and the produced water vapor is directed into the activation zone.

This apparatus is not as such applicable to a moist residue but only to a dried residue.

The object of the present invention is therefore to provide a simpler and more economical process than the previous ones for the production of coke and activated carbon from a moist organic substance such as moist furfural residue, milled peat or crushed block peat.

Relatively dry residue can also be treated by the process and apparatus according to the present invention, provided that the residue is first moistened.

The main characteristics of the invention are given in accompanying Claim 1.

The process and apparatus according to the present invention can be used for producing activated carbon and coke directly in one stage from moist, finely-divided organic substances.

According to the invention, the moist raw material and the auxiliary fuel to be reduction burned and possible the flue gases obtained from the outlet end of the furnace are brought into contact with each other by feeding them into a cylinder furnace operating according to the co-current principle, in which water is first released from the moist raw material in the drying zone, and when the dried raw material is heated further, combustible gases and tar are released from it in the coking zone.

These are reduction burned by means of air or oxygen, or a mixture of the same, fed in at different points of the mantle of the cylinder furnace, and the temperature and the composition of the gas are adjusted so as to produce either activated carbon or coke as the final product.

Considerable advantages over conventional activation processes carried out using water vapor have been gained by the activation process and apparatus according to the present invention.

The profitability of the process and the apparatus are increased by, for example, the following advantages: the use of inexpensive moist and finely-divided residues and raw materials, a single-stage combined drying, coking and activation process, the elimination of separate feed of water vapor into the activation zone, the obtaining of products which are already classified into different particle size categories, some being granular and some pulverous, the simplicity and easy control of the process, and an apparatus which is uncomplicated and reliable in operation.

The invention is described below in more detail with reference to the accompanying drawings, in which Figure 1 depicts a cross sectioned side view of an apparatus for carrying out the drying, coking and activation process according to the invention, and Figure 2 depicts a cross-sectioned side view of a cylinder furnace for carrying out the drying and coking process according to the invention.

In Figure 1, moist furfural residue with a water content of approx. 4050% is fed in by means of feeder 1 and further along the pipe 2 to the leading end of the cylinder furnace 3. At the leading end of the cylinder furnace 3 there is, furthermore, a burner 4, in which a mixture of a fuel; such as naturalgas, and air and/or oxygen is reduction burned. The fuel used can also be oil, cycled gas or the material being treated. Several longitudinal lifting devices 5 have been attached to the interior wall of the leading end of the cylinder furnace 3, peripherally at a distance from each other, for mixing the moist furfural residue and the hot flue gases with each other in order to dry the furfural residue in the drying zone 6.From the drying zone 6, the dried furfural residue and the moist flue gases are directed into the coking zone 7, which has air nozzles 8 for feeding additional air into the coking zone 7 for the coking of the dried furfural residue and for burning the combustible gases produced during the coking.

In the embodiment depicted in Figure 1, several lifting devices 5' have been fitted immediately beyond the coking zone 7 longitudinally on the interior wall of the cylinder furnace 3, peripherally at a distance from each other, for mixing the coke and the moist, hot gases emerging from the coking zone 7, in order to activate the coke in the activation zone 9. At the trailing end of the cylinder furnace 3 there is, furthermore, a cooling zone 10 and an end chamber 1 through which the coarsest fraction 1 2 of the product is withdrawn from the cylinder.

The mixture of the gas and the product contained in it is directed into the gas-cooling system in the pipe 14. From the gas-cooling system 13, where the finer fraction 1 7 of the product is separated, the remainder is directed further along the pipe 1 5 into the bag filter 16, where the finest fraction 1 7' of the product is separated from the gases, and the gases are directed into the flue 20 via the outlet pipe 19 provided with a blower 18.

The outlet gas of the cylinder furnace 3 contains a large amount of combustible constituents, and most of these can be burned prior to the gas-cooling apparatus 13, or the waste heat vessel, whereby this energy can be recovered. Such an after-burner is shown in Figure 1 and indicated by 21. The combustible constituents can also be burned after the pulverous activated carbon 1 7 has been separated from the gas.

Part of the outlet gas of the cylinder furnace can also be cycled. In this case the outlet gas emerging from the furnace can be directed into a cyclone (not shown in the figures), where the dusts are separated from it and part of the gas is recycled to the feeding end of the furnace and an oxygen-bearing gas is added to the gas in order to burn it. The remainder of the gas passes to cooling and dust removal. The cycled gas fed to the feeding end of the furnace can, of course, also be recovered from the outlet gas after the cooling and dust separation.

When only coke is desired, the lifting devices 5' fitted in the apparatus of Figure 1 next in succession to the coking zone 7 can be eliminated. Activation is an endothermal reaction and requires, in order to take place, an effective mixing of the gas and the material. On the other hand, coking does not require such effective mixing, and especially if the intention is to perform the coking at a high temperature, 900 1000 C, the mixing must be eliminated in order to produce coke and not activated carbon. When dried furfural residue is coked, the retention period in the furnace is shorter and the coke does not have time to become activated. In this case the capacity of the cylinder furnace 3 can also be adjusted to a higher level.

The fuel can be burned with the aid of either air or oxygen, or a mixture of the same. When a concentrated gas is desired, for example for gassing or for the production of a high-grade activated carbon, the burning can be carried out with pure oxygen.

The cylinder furnace depicted in Figure 2 differs from that depicted in Figure 1 in that it has no lifting devices 5' immediately beyond the coking zone 7, i.e. the activation zone 9 has been eliminated.

The process is controlled by regulating the retention period of the material and the temperature and the composition of the gas. If necessary, the moisture content of the feed can be decreased by drying the feed by means of outlet gas or, if the feed is too dry for activation, its moisture content can be increased. The amount of auxiliary fuel required by the process can be decreased by burning part of the feed, by burning a larger proportion of the volatile constituents of the feed, by pre-heating the combustion air indirectly by means of outlet gases, or by cycling part of the outlet gases.

The invention is described below in more detail with the aid of examples.

Example 1 Furfural residue which contained volatiles 78%, its analysis being C 49% and ash 1.7% of the dry matter, was fed into a cylinder furnace having a length of 10.6 m and an inner diameter of 0.8 m.

The moisture content of the furfural residue was 52.5% and the particle size of the dry matter was 94% under 10 mm and 8% under 0.42 mm. Moist furfural residue was fed into the cylinder furnace at 151 kg/h, and butane was fed from the burner to the leading end as an auxiliary fuel at 14.8 kg/h, the air rate being 1 74 m3/NTP/h. Air was fed into the coking zone at three points of the cylinder mantle, a total of 98 m3/NTP/h. The temperature of the cylinder in the activation zone was 9300C, and the dry gas contained CO 3% and H2 3%. The rotational velocity of the cylinder was 2 r/m. The gas emerging from the cylinder was burned in the end chamber of the outlet end by feeding air into it at 284 m3 NTP/h and butane from the burner as an auxiliary fuel at 5.1 kg/h.

The product obtained from the cylinder was 3.0 kg/h activated carbon with a BET surface area of 659 m2/g and an ash content of 17.2%; from the waste heat vessel 0.73 kg/h product with a BET surface area of 664 m2/g and an ash content of 20.4%, and from the bag filter 0.31 kg/h product with a BET surface area of 246 m2/g and an ash content of 45.6%.

Example 2 Furfural residue containing volatiles 78% and ash 1.7% of the dry matter was fed into a cylinder furnace according to Example 1. The moisture content of the furfural residue was 41.1% and its particle size 96% under 10 mm and 11% under 0.42 mm.

Moist furfural residue was fed into the cylinder furnace at 1 80 kg/h and butane was fed from the burner into the feeding end as an auxiliary fuel at 20.6 kg/h, the air rate being 253 m3 NTP/h. Air was fed into the coking zone at three points of the cylinder mantle, in total 54 m3 NTP/h. The cylinder temperature in the activation zone was 9000C, and the dry gas contained CO 4% and H2 4%. The gas emerging from the cylinder was burned in accordance with Example 1 by directing into it air at 362 m3 NTP/h and butane from the burner as an auxiliary fuel at 5.0 kg/h.

The product obtained from the cylinder was 1.9 kg/h activated carbon with a BET surface area of 652 m2/g, an ash content of 6.0% when washed, from the waste heat vessel 3.2 kg/h product with a BET surface area of 601 m2/g and an ash content of 15.5%, from the bag filter 0.3 kg/h product with a BET surface area of 519 m2/g and an ash content of 15.7%.

Example 3 Furfural residue containing volatiles 78%, its analysis being C 46% and ash 1.2% of the dry matter, was fed into a cylinder furnace according to the previous examples. The moisture content of the furfural residue was 43.8% and the particle size of the dry matter was 94% under 10 mm and 8% under 0.42 mm. Moist furfural residue was fed into the cylinder furnace at 1 50 kg/h and butane was fed to the feeding end fromthe burner as an auxiliary fuel at 1 5.1 kg/h, the air rate being 178 m3 NTP/h. A total of 87 m3 NTP/h air was fed into the coking zone at three points of the mantle surface. The cylinder temperature in the activation zone was 9400 C, and the dry gas contained CO 3% and H2 3%.

The gas emerging from the cylinder was burned in accordance with the previous examples by feeding into it air at 245 m3 NTP/h and butane from the burner as an auxiliary fuel at 5.1 kg/h.

The product obtained from the cylinder was activated carbon with a BET surface area of 801 m2/g and an ash content of 15.5%, from the waste heat vessel a product with a BET surface area of 664 m2/g and an ash content of 16.9%, and from the bag filter a product with a BET surface area of 257 m2/g and an ash content of 50.7%.

Claims

1. A process for the production of activated carbon or coke from a moist organic substance, which comprises mixing the moist organic substance with hot flue gas to dry it, coking the dried organic substance by reduction-burning of the volatile constituents thereof with an oxygenbearing gas, separating the coked substance from the gas, or activating it by mixing it with the hot, moist gas from the coking operation, without separate addition of water vapour, and then separating the activated carbon from the gas, the drying and coking or the drying, coking and activation, respectively being performed by co current passage of the organic substance and gas in a continuous zone.

2. A process according to Claim 1, wherein the starting organic substance has a moisture content of 3070% by weight.

3. A process according to Claim 2, wherein the starting organic substance is a residue from the production of furfural.

4. A process according to Claim 1,2 or 3, wherein effluent gas from the process is recycled to the drying step.

5. A process according to Claim 1 carried out substantially as hereinbefore described with reference to Figure 1 or 2 of the accompanying drawings.

6. A substantially cylindrical furnace suitable for carrying out a process according to Claim 1, comprising means for directing the moist organic substance and the hot flue gas into a drying zone of the furnace equipped with means for mixing the moist organic substance with the flue gas, means for directing the oxygen-bearing gas into a coking zone of the furnace downstream of the drying zone, exit means for removal of effluent gas and coke or activated carbon from the furnace, the drying and coking zones being arranged to form a single continuous zone in the furnace.

7. A furnace according to Claim 6 which further comprises, downstream of the coking zone, in an activation zone which is continuous therewith, mixing means for mixing the gas from the coking zone with the coke, to produce activated carbon therefrom.

8. A furnace according to Claim 6 or 7, wherein the mixing means in the drying and/or activation zones are devices attached substantially normally to the interior wall of the furnace for lifting the organic substance.

9. A furnace according to Claim 6, 7 or 8 arranged slopingly for downward and horizontal passage of the organic substance therein.

10. Apparatus for carrying out a process according to Claim 1 comprising a furnace claimed in Claim 6, 7, 8 or 9 and means for burning effluent gas emerging from the furnace.

11. Apparatus for carrying out a process according to Claim 6, 7, 8 or 9 and means for cooling the hot, effluent gas from the furnace and for separating and recovering dust present in the gas in one or more fractions.

12. Apparatus for carrying out a process according to Claim 1 constructed and arranged substantially as hereinbefore described with reference to and as illustrated in Figure 1 or 2 of the accompanying drawings.

13. A process for the production of activated carbon or coke from a moist organic substance, wherein a moist organic substance is first mixed with hot flue gases in the drying zone, whereafter the dried organic substance and an oxygen bearing gas are directed into the coking zone for a reduction burning of the volatile constituents of the organic substance at an elevated temperature, then the coked substance is separated from the gas, or the material emerging from the coking zone is directed into the activation zone, where it is mixed with hot, moist gases, and finally the gases are separated from the activated carbon, characterized in that the drying, coking and activation, or the drying and coking, are performed according to the co-current principle in one and the same gas chamber and the activation is performed without a separate addition of water vapor.

14. A cylinder furnace intended for carrying out the process according to Claim 13, characterized in that it has members for directing the moist organic substance and the hot flue gases into a drying zone in the leading end of the furnace, the drying zone having mixing members, members for withdrawing the coke or activated carbon and the gases originating in the reduction burning at the trailing end of the furnace, members for directing the oxygen-bearing gas into the coking zone which is subsequent to the drying zone, the furnace having possibly been fitted with mixing members next in succession for mixing the hot, moist gas originating in the coking zone with coke in order to activate the coke, thereby producing activated carbon.