• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1. METHOD OF CONTINUOUS GASIFICATION OF PARTICLES OF A SOLID UGZER-CONTAINING MATERIAL in a rotary kiln, including a continuous supply of source material from its input to the kiln to form a layer of material, supplying an oxidizing medium containing steam, gradually heating the material to 1093 ° C during the rotating slot inclined from the upstream side of the source material to the unloading side of the material with the formation of gases containing hydrocarbons and gases that do not contain hydrocarbons, the output of these gases from the side of unloading solid The remaining residue is also from the input side of the source material, characterized in that, in order to increase the calorific value of the gases produced and prevent resin deposition on the equipment surfaces, the temperature of the gases withdrawn from the source loading side into the furnace is maintained at a level at which the resin will condense, preferably within 538-687С by adjusting the amount of non-hydrocarbon gases that are removed from the furnace on both sides. 2. Method pop. 1, which is also distinguished by the fact that with a decrease in temperature of gases discharged from the input side of materials below 538 C they reduce the flow of gases discharged from the unloading side of the material and increase the flow of gases discharged from the input side of the source material. 3. The method according to claim 1, characterized in that when g is lowered, the temperature of the gases discharged from the material inlet side, expelling 687 C CO increases the gas flow, is discharged from the unloading material, and reduces the gas flow discharged from the input side of the source material . 4. Method pop. 1.2 and 3, characterized in that for every 0.454 kg / h of gas withdrawn from the furnace, on the discharge side of the material, 1.6161 kg / h of gas from the furnace on the input side of the material into the furnace is delivered. 5. Method according to paragraphs. 1-4, characterized in that the oxidizing medium, which does not contain steam, is introduced into a part of the layer having a temperature below. 6. The method according to claims. 1-5, characterized in that the oxidizing medium is introduced into the furnace under pressure, providing an excess of 1.406 atm. In the furnace.
    公开号:SU1114342A3
    申请号:SU823441351
    申请日:1982-05-17
    公开日:1984-09-15
    发明作者:Джордж Гарсайд Питер
    申请人:Аллис-Чалмерс Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the anhydrous method of gasifying coal or other carbonaceous materials in a rotary kiln.
    Coal gasification methods conducted in an inclined rotary kiln have several advantages. Rotating furnaces for coal gasification can be built to very large sizes, their productivity can be easily controlled by adjusting the speed of rotation. The material fed to the furnace may not be screened to any specific size, as the rotating furnace can work both with large pieces, and with very small particles. - A large chamber can be used to smooth out the coking coal swellings. The constant movement of portions of coal due to the rotation of the furnace provides almost uniform temperatures inside the layer along the entire length of the furnace.
    A known method of continuous gasification of particles of solid carbon-containing material in a rotary kiln, including the continuous supply of raw material from its input into the furnace with the formation of a layer of material, the flow of an oxidizing medium containing steam, the gradual heating of the material to 1093 C in a rotary kiln tilted down from the input side of the source material to the discharge side of the material with the formation of gases containing hydrocarbons, and gases that do not contain hydrocarbons, the withdrawal of the specified gas from the discharge side the solid residue and from the input side of the source material 13, the purpose of the invention is to increase the calorific value of the gases produced and to prevent the deposition of resin on equipment surfaces, i.e. creating a method for gasifying coal in a rotary kiln, which has additional advantages, foremost among which is the production of fuel gases that are extracted from coal
    greater calorific value, than hidden chemical energy,. is released when burning the fuel gas in the form of thermal energy in devices that are not associated with the production of gas from coal, such as a steam boiler. Heat generation is limited by the rate at which Obn-b can achieve substantial heat recovery for other economically viable applications. .
    According to the proposed method, both tar-containing gas and non-tar gas are produced. A tar-free gas is used to maintain the tar-containing gas at temperatures high enough to prevent the resins from condensing on the surfaces of the gasification process equipment.
    In accordance with the inventive method, the oxidizing gas and steam is injected through a preheated layer of carbon-containing material, which turns over in a rotary kiln due to its rotation. In this case, gas and steam are supplied in quantities that are regulated in such a way as to heat and ensure separation of the gas-containing gas from the material. Which is passed over the material entering the furnace in order to transfer part of the heat content from this gas and thus provide a preliminary heating of the incoming material - raw material. This preheating gas is then removed from the furnace from the input side of the solid material, and the gas containing no resin is produced from carbon or carbon from the carbonaceous material and this gas containing no resin is removed from the furnace from the discharge side of the solid material. at a temperature ,. approximately equal to 1038 ° C. The flow rate of the gas flows emitted from the furnace is further controlled in a certain proportion so that a part of the gas containing no resin and having a temperature of approximately 1038 ° G will be mixed with the lower temperature gas containing the resin and leaving the rotating furnace input of solid materials in an amount sufficient to maintain
    The temperature of these mixed gases is high enough to avoid. condensation of resins on technological equipment surfaces. gasification. Remaining part
    the gas stream having a high temperature is discharged as a gas that does not contain balsam from the furnace from the sides. unloading solid materials. The process parameters for regulating the ratio of gas flows coming from each side of the furnace may include: maintaining the temperature of gases removed from the furnace from the input of solid materials, approximately equal to 538 ° C, maintaining the methane content of gas in the furnace from the furnace from the side unloading of solid materials, in the range of 0-0,1%. As can be seen from the examples below, meeting these requirements may require the removal of 1,361 kg / h of gas from the furnace from the input of solid materials relative to 0.454 kg / h of gas removed from the furnace from the discharge of solid materials, and this ratio may be from about 2: 1 to 4: 1 for bituminous coals, while for sub-bituminous (brown) coals, without pre-drying, it is necessary to mix almost 100% high-temperature 9 non-resinous gas with low-temperature gas containing resin, with so that th gas which vgoodits from the furnace by the supply of solid materials and comprises a resin temperature had significantly (warranty) prevsh1ayuschuyu condensation temperature. Devices designed to determine the methane content are produced promptly, but there are no devices that continuously determine the resin content in the gas. In cases where the content of methane in the gas recovered from the furnace on the side of the discharge of solid material exceeds 0.1%, the resins and other condensable hydrocarbons can probably be in the gas. Thus, the measurement of the methane content determines the presence or absence of unwanted resins and other condensable hydrocarbons in the high-temperature gas that is removed from the furnace from the side, the discharge of solid materials. FIG. Figure 1 shows a schematic of the installation and a drawing of a rotary kiln for coal gasification; in fig. 2 is a section A-A in FIG. one; in fig. 3 - the dependence of the magnitude of the condensation of the resin from the gas stream containing the resin of FIG. 4 is a graph showing the temperature change of the particles of the solid carbonaceous material subjected to gasification and the temperature change of the gases above the bed as a part of the solid material passes along the rotary kiln. The gasification unit comprises an inclined rotary kiln 1 having a refractory lined wall. Coal or other solid carbon-containing material is fed through supply line 2 to more. the high end 3 of the furnace 1 through the feed nozzle 4. The furnace 1 is inclined from the top down from the end 3 of the furnace, intended for the input of the source material, to the end 5 of the furnace 1, intended for the production of solid material - ash. This furnace tilt, together with the rotation of the furnace body 1, results in the formation of a coal layer 6 inside the refractory lined furnace body 1 and a slow movement from top to bottom of this material layer due to the furnace tilting during coal gasification. The end 3 of the furnace 1, intended for the input of the source material, is equipped with a fixed exhaust hood 7, having a nozzle 8, intended for the removal of gas. The end 5 of the furnace 1, designed for ash extraction, is equipped with a fixed exhaust hood 9. The exhaust hood 9 for discharging the ash has a branch pipe 10 for removing the gas and a channel 11 for discharging the ash. Burner 12 installed in exhaust hood .9 is designed to preheat the furnace and coal to operating temperature during the start-up of the installation. For the burner, combustible gas or any other suitable fuel may be used. When the gasification device is operating with a pressure inside the furnace body exceeding atmospheric, the system for supplying air and steam to the rotating body of the furnace 1 includes a blower 13 for supplying pressurized air connected to the air supply pipe 14, a source of compressed steam (not shown) and a pipe 15 for steam supply. The pipes 14 and 15 pass through the fixed support plate 16. The fixed collection Top 17, abutting against the plate 16, and (FIG. 2) has arcuate channels (slots) 18 and 19. The collector 17 is connected to the side opposite the fixed mounting plate 16 with a pipe support 20 mounted on the furnace body 1 and rotating together with the furnace body 1. A plurality of circumferentially and axially extending tubes 21 and 22 are mounted on the pipe support 20, with the tubes 21 and 22 extending towards the end of the furnace 3 intended for loading solid material into the furnace 1. Each of the tubes 21 is connected to a plurality of radial channels 23, which are connected to the openings 24 that open radially inward of the furnace 1 through a refractory lining 25 for connecting the pipelines to the inside of the furnace. The channels 23 pass under the layer of material 6 when the furnace body 1 rotates. As the furnace body 1 rotates, the furnace 1 and the pipe support 20 have tubes 21 that pass through an arcuate channel 18 located in a fixed manifold 17, thereby ensuring the flow of air flowing from the pipe 14 through the channel 18 into one or more tubes 21, which pass along the channel 18. The air then exits the tubes 21 through the radial channels 23 and the apertures 24 and then through the layer 6 of material in the furnace. The system for supplying and distributing steam entering through conduit 15 into pipes 26 is similar to the system for supplying and distributing air described above. Each of the pipes 26 is connected to a set of radial channels 27, which, in turn, are connected to the channels 28 and to the openings. Due to the fact that the furnace 1 rotates, this furnace and the furnace support 20 extend along the arcuate channel 19 in the fixed collector 17c in order to allow the flow of steam entering the pipeline 15 through the channel 19 into one or more tubes 22 passing by channel 19. The vapor then flows from the tubes 22 through the radial channels 27 and 23 and the orifices 29, displacing with the air as it passes through the layer of material 6 that is in the furnace. 2 Valves (not shown) may be installed on tubes 21 and 22 passing along the furnace and / or on radially passing channels 23, 27, and / or on fluid supply lines in order to change the arrangement and number of holes 24, to ensure the operation of the furnace in accordance with the proposed method and to supply air and steam, as is necessary when working with various carbon-containing materials subjected to gasification. Nozzles can be installed in each of the holes 29, (not shown). Fuel gas flows simultaneously from the end 3 of the loading of solid material (coal) into the furnace 1 and from the side of the loading of solid material (ash) from the furnace 1. The flow of exhaust gas released from the furnace 1 from the side of supply of solid material. It passes through the inlet 8 of the gas and its flow is controlled by the valve 30. The flow of exhaust gas, which is free from gas. By the inlet 8, enters the cyclone separator 31, designed to separate solid particles from the gas. The waste gas flows from the cyclone separator 31 through line 32 to a device for further purification (not shown). A device for further purification of the gas supplied through conduit 32 may include a scrubber 33 and a hydrogen sulfide removal system 34. Particles removed from the gases using separator 31 can be returned by feeding these particles through conduit 35 to feed 36. into furnace 1 for gasification. The flow rate of gas discharged from the end 5 of the discharge of solid material (ash) from the furnace 1 and passing through the nozzle 10 is controlled by the valve 37. The waste gas flow through the nozzle 10 is fed into the cyclone separator 38, designed to separate solid particles from the gas, then the waste gas containing no particles of solid material from separator 38 is fed through conduit 39 to heat exchanger 40, which is designed to extract heat from this gas, for example, by generating steam. Next, the gas from the heat exchanger
    40 enters the scrubber 41, which may be the same as the scrubber 33, and then into the system 34 to remove the hydrogen sulfide. Gas from the hydrogen sulfide removal system 34 may be fed to a steam boiler burner or a mixed cycle power plant (not shown). Particles of solid material, extracted from gases with the help of separator 38, pass through pipe 42 and enter channel 11, which is intended for unloading EOLA from furnace 1.
    The installation works as follows.
    The burner 12 is ignited in order to heat up the lining 25 of the rotary kiln 1 of hoods 7 and 9, as well as nozzles 8 and 10, designed to discharge the produced gas. After the inner surface of the refractory lining is heated to 816982 G, the coal particles are supplied through the feed pipe 4 to the furnace 1. When the furnace is partially filled and the coal layer 6 almost closes the entire length of the furnace, air begins to flow and steam through the holes 24 to the layer 6, since the openings 24 are located under this layer, and the burner 12 is turned off. The temperature of coal coal moving downward due to the inclination of the furnace 1 quickly increases from 871 to near the end 5 of the discharge of solid materials from the furnace 1 and the ratio between the flow of air and steam in the mixture introduced into the furnace through the holes 24 is adjusted to maintaining the required temperatures.
    The air supplied by the blower 13 under pressure passes through the pipeline 14 through the arcuate channel 18 in the manifold 17 (FIG. 2) and then enters each of these tubes 21 located in the direction along the furnace 1 (shown only in FIG. 1), passing by channel 18 as a result of rotation of the furnace body 1. From the tubes 21, the air passes through the radial channels 23 of the holes 24 into the layer of material 6.
    The steam produced by the steam generator (not shown), under pressure passes through the pipe 15, the arcuate channel 19 in the collector 17 (figure 2) and enters each of the long tubes 26 located in the direction along the furnace 1 (figure 1) and passing passing through channel 19 as the kiln case 1 rotates. From the tubes 26, the steam passes through the radial channels 27, which are connected to the channels 23, resulting in a mixture consisting of air and steam, which then passes through the holes 29 into the layer of material 6. It should be noted that the steam pipes are not proc d m in the direction of feed of the furnace input 1 as far as it is the case for channels 23, the air supply, thereby providing administered only air in the areas material layer disposed on the downstream of the material before the layer portions through which is passed a mixture of air and steam.
    The vapor pressure and air pressure inside the furnace 1 is regulated in such a way as to maintain the gas pressure in the furnace at least 1.406 kg / cm and preferably 4.22–12.66 kg / cm (excluding pressure, i.e., pressure exceeding external pressure). Atmosphere pressure). The output of such pressurized gases at both ends 3 and 5 of the furnace 1 can be controlled by means of control valves 30 and 37.
    The proposed method provides simultaneous and continuous production of two completely different flows of fuel gas and their injection from two opposite ends of one furnace 1. The first gas flow, which contains almost all the resins formed as a result of the method, is formed as the coal heats up from 205 to and, if this gas is removed from the side of the loading of solid material into the furnace 1 without the addition of gases having a higher temperature, then this gas is at tempedatures, in the range of which The vapor condensation takes place (Fig. 3).
    The second gas stream is formed in an atmosphere containing steam and air after the coal is heated to a temperature in excess of about 871 ° C and converted to charred COAL. This second gas, discharged from the discharge of solid material from the furnace 1, has a relatively high temperature (about) and contains almost no resin. Heat can be extracted from this tar-free gas, and steam can be obtained using heat exchanger 40 only after simple purification from particles of solid material, which can be carried out using a cyclone separator 38. The ratio between the flow rate of gas removed from the side of the solid charge. materials into the furnace 1, and the gas supplied by the discharge of solid material from the furnace 1, is adjustable GREATNY proportional to these costs and is realized by rearranging the control valves 30 and 37 in such a way Ohm, that at least part of the gas having a temperature of 1038 ° C and not containing resin is mixed with the gas containing the resin and moving towards the inlet side of the material of the furnace 1, and this high-temperature gas is used in an amount sufficient to maintain the resulting gas the mixture at a temperature of about 538 ° C, which is quite high and avoids the condensation of resins on the surfaces of the sulfur-free equipment, i.e. furnaces, gas valves, etc. FIG. 3 shows, but what is very insignificant in resin condensation at temperatures exceeding 371 ° C, however, even insignificant condensation of the resin during long periods of time leads to the formation of significant deposits of resin on the lining of the furnace 1 and inside valves 30 and 37, which prep It contributes to the normal operation of the process equipment and has a negative effect on the process. For trouble-free operation over an extended period of time, the temperature of the gases removed from the solid materials input side of the furnace is approximately 538 ° C, which ensures the best offset of these two gas streams. However, in the event that gases are removed with co. The sides of the input of solid material into the furnace 1 at temperature ranges significantly exceed the temperature required to prevent condensation of the resin on the equipment surfaces. 1 2 this could mean that the high-temperature gas is needlessly taken from the gas stream, from which heat can be extracted after simply removing solid particles from the cyclone separator 38. The process can be explained by graphs of the temperature of the gas above the bed , and the temperature of the layer along the length of the furnace, i.e. with respect to the path of transfer of solid material from the side of loading solid material into furnace 1 from the side of unloading solid material from furnace 1 (Fig. 4). FIG. 4, it is proved that particles of solid coal moving through furnace 1 are dried in the temperature range of 93-120 ° C. The coal particles are then heated to a temperature of approximately 205 ° C and higher, and pass over openings 24, through which only air is supplied, while the coal begins to draw in gas that contains tar (sometimes called coal gas) and almost completely It is emitted from coal during that period of time when the temperature increases to 871 ° C or slightly higher. The complete release of volatile components turns coal into charred coal, as the temperature of the charred coal rises in the vapor-air atmosphere provided by the flow of steam through the channels 27 (Fig. 1), and this temperature reaches a value equal to Bbmie, the charred coal absorbs gas , (sometimes called water gas) does not contain 1st resin. Since the furnace 1 operates under pressure, by opening the valves 30 and 37 (FIG. 1), it is possible to provide the output and control of the flow rate of the gas output on both sides of the furnace 1. The valves 30 and 37 are opened in order to remove all the gas containing the resin , plus a certain amount of gas that does not contain tar, from the zone: a gas stream moving in two directions (in Fig. 4, this zone is indicated as a shaded area). The temperature of the gas containing the resin (FIG. 4) decreases quite quickly as this gas moves to the loading side of the solid material of the furnace 1 and this gas preheats the incoming coal moving and turning over towards the discharge side of the solid material from the furnace 1 with the exception of a certain part of gas that does not contain tar and is free from the shaded zone, from the side of solid material loading into the furnace 1, together with the gas containing the resin, with gases removed from the furnace from the side of solid mat loading RIA fishing should be cooled to below the pace ture 538S. The resin condenses according to the relationship shown in FIG. 3. The exact position of the valves 30 and 37 (figure 1) at any time should be such as to maintain the temperature of the gases removed from the furnace from the input of solid material equal to a given temperature, t. Approximately equal to 538 ° C so that Avoid condensation of the resin on the surface of the equipment. For most coals, as well as for all coals, maintaining a temperature of approximately 538 ° C will also ensure the removal of tar-free gases from the furnace from the outlet of solid material from the furnace in such a way that heat can be removed from the stream - gas by vaporization using heat exchanger 40 immediately after separation (purification) of solid particles from the gas using a cyclone separator 38 and before being fed to the scrubber 41 and to the hydrogen sulfide removal system 34. Another parameter used when removing gas from the furnace from the discharge side of the solid material and making it clear that this gas does not contain tar is the concentration of methane in this gas. There are industrial instruments for determining methane content in the range of 0-6.1%, which indicates the absence of tar in the gas. . . The proposed method maximizes the production of fuel gas with a certain calorific value in the form of latent chemical energy, which can be consumed as thermal energy when this fuel gas is combusted, while avoiding the condensation of tar in the gas e removed from the feed side of the materials into the furnace. Example 1. Il 6 coal is gasified and is approximate in%: Moisture12 Volatile material, 33.3 Sv carbon (coke) 41.7 Ash13 composition, without taking into account the fuel and ash,%: Hydrogen Carbon Oxygen borax parameters and results: kg / h with Coal.18921 Zola291038 Gas output from the solid material supply side514538 Gas output from the discharge side of solid material1771038 Steam 110246 Air 425246 example 2. Gas from Pit 8 coal having an approximate value of,% Moisture4.4 Volatile material39, 5 Bound carbon (coke) 48.6 Ash7.5 cement composition excluding fuel and ash,%: Sulfur Hydrogen Carbon Nitrogen Oxygen parameters and results of gas extracted from freeze of solid raw material per 1 kg of feed -in the stove, is equal to g): Coal163 21 Ash14.5 1038 Gas output from the solid material supply side 433 538 Gas output from the discharge side of solid material 245 1038 Steam110 246 Air 425 246 Example 3. Wyoming pulverized river half-line coal having an approximate composition,%: Moisture30.4 Flying material31, 1. Bound carbon (coke) 32.1 Ash 6j4 Elemental composition excluding moisture and ash content,%: Sulfur, 0.8 Hydrogen5.5 Carbon75.7 Nitrogen1.0 Oxygen17.0 Performance parameters and results (amount of gas, recovered from the range of supply of solid raw materials, to 1 coal supplied to the furnace, it is equal to 3.1 kg): kg / h С Coal245 21 Zola20 1038 Gas output from the stand-. RODS of solid material supply757 .538
    Table 1 2 Gas output from solid material discharge Steam Air Table. 1 shows the composition of gases (in examples 1-3) discharged from the input and output ends of the furnace. In tab. Figure 2 shows the calorific value of the gases, excluding the resin, and the amount of resin in Examples 1-3. It is not practical to build an enterprise for coal gasification if there is only the coal grade specified in Example 3. However, if coal is supplied that has only a higher humidity. the low carbon content to be processed, the operator can control the location of the separation of the gas stream that does not contain tar, and this location can be at a point where, with efficient processing of such coal, no gas is withdrawn, but containing resin. In Example 3, the process is carried out in such a way that all gases are vented from the input side of the starting material. The advantages of the proposed method in comparison with the well-known technical solutions are retained. Resin deposition on the walls of the equipment is prevented. In addition, the method allows to extract a greater amount of heat from a ton of coal as compared to the known methods, which suggest burning the resin in order to prevent its deposition on the equipment walls.
    21 16
    17 19
    WITH
    20 16
    16 19
    25 14
    1030 1315
    1200
    Amount of resin, kg / h
    19.5
    Continuation of table 1
    table 2
    1110
    1000
    29.5
    14.9
    ///
    one %
    权利要求:
    Claims (6)
    [1]
    1. THE METHOD OF CONTINUOUS GASIFICATION OF PARTICLES OF A SOLID CARBON-CONTAINING MATERIAL in a rotary kiln, including the continuous supply of the starting material from the side of its introduction into the kiln with the formation of a layer of material, the supply of an oxidizing medium containing steam, the gradual heating of the material to 1093 ° C in a rotary kiln, inclined from above down from the input side of the source material to the discharge side of the material with the formation of gases containing hydrocarbons and gases not containing hydrocarbons, the output of these gases from the discharge side of the solid attack and from the input side of the source material, characterized in that, in order to increase the calorific value of the obtained gases and prevent the deposition of resin on the surfaces of the equipment, the temperature of the gases discharged from the side of loading of the source material into the furnace is maintained at a level at which condensation will not occur resins, preferably between 538-687 ° C., by controlling the amount of hydrocarbon-free gases discharged from the furnace on both sides thereof.
    [2]
    2. The method according to claim 1, characterized in that when the temperature of the gases discharged from the input side of the materials decreases below 538 ° C, the flow rate of gases discharged from the discharge side of the material is decreased and the flow rate of gases discharged from the input side of the source material is increased.
    [3]
    3. The method according to claim 1, characterized in that when the temperature of the gases discharged from the input side of the material drops above 687 ° C, the flow rate of gases discharged from the discharge side of the material is increased and the flow rate of gases discharged from the input side of the source material is decreased.
    [4]
    4. The way popp. 1, 2 and 3, characterized in that for every 0.454 kg / h of gas discharged from the furnace from the discharge side of the material, 1.361 kg / h of gas is removed from the furnace from the input side of the material into the furnace.
    [5]
    5. The method according to PP. 1-4, characterized in that the oxidizing medium, not containing steam, is introduced into part of the layer having a temperature below 1038 ° C.
    [6]
    6. The method according to PP. 1-5, characterized in that the oxidizing medium is introduced into the furnace under pressure, providing an overpressure in the furnace of 1.406 ati.
    m SU <„, 1114342
    111
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    同族专利:
    公开号 | 公开日
    DE3216836C2|1991-06-20|
    GB2099014A|1982-12-01|
    GB2099014B|1984-10-24|
    PL137643B1|1986-07-31|
    IN157946B|1986-07-26|
    US4374650A|1983-02-22|
    PL236475A1|1983-01-17|
    JPS581791A|1983-01-07|
    CA1169657A|1984-06-26|
    ZA823012B|1983-06-29|
    FI821729A0|1982-05-17|
    SE8202808L|1982-11-19|
    FR2505864B1|1987-12-24|
    IT1197428B|1988-11-30|
    SE453099B|1988-01-11|
    IT8248434D0|1982-05-17|
    FR2505864A1|1982-11-19|
    AU8342082A|1982-11-25|
    AU545077B2|1985-06-27|
    DE3216836A1|1982-12-02|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/264,479|US4374650A|1981-05-18|1981-05-18|Bi-flow rotary kiln coal gasification process|
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