• 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:
    An apparatus and method for performing a continuous thermal treatment of organic carbonaceous materials under controlled pressure in which the feed material is introduced into the system in the form of a slurry, and the level of liquid is maintained at a preselected operating level, serving as a gas-tight seal. The feed material is conveyed upwardly of the liquid operating level and is thereafter introduced into a reaction chamber in which it is heated to within a controlled elevated temperature range under controlled pressure in a manner to effect vaporization of at least a portion of the volatile substances therein, forming a gaseous phase composed of condensible and noncondensible vapors. The gaseous phase is withdrawn from the reaction chamber in a direction countercurrent to the travel of the feed material and in heat exchange relationship therewith, effecting condensation of the condensible phase and transport of the noncondensible phase, and is extracted from the system through a discharge port disposed above the liquid operating level. The thermally reacted product is cooled and transferred from the reaction chamber into a receiving chamber from which it is extracted continuously or intermittently.
    公开号:SU1085509A3
    申请号:SU782669956
    申请日:1978-09-12
    公开日:1984-04-07
    发明作者:Коппельман Эдвард；Гордон Меррэй Роберт
    申请人:Эдвард Коппельман (СГА)；
    IPC主号:
    专利说明:

    The invention relates to the chemical industry, in particular to methods and devices for the heat treatment of organic carbonaceous materials to produce gases and a solid product. The known method of heat treatment of organic carbon materials, including mixing the source material with a liquid, (Transportation of the mixture from the bottom up through a layer of liquid with an adjustable level, the supply of wet material to the reaction zone, its processing with increased pressure and temperature to obtain gases and solid product ij It is also known a device for the heat treatment of organic carbonaceous materials, comprising successively installed means for mixing the original mother. la with liquid, transport chamber with liquid, installed at an angle to the horizontal plane and having means for transporting NIN material and means for adjusting the level of liquid, a reaction chamber connected to the upper part with the upper part of the transport to the measure and having means for removing solid product and a pipe for water gas fij. The disadvantages of the known method and device are that they inefficiently use the energy supplied and released in the process e. The aim of the invention is to improve e process efficiency. The goal is achieved by the fact that according to the method of thermal processing of organic carbon materials, including mixing the source material with a liquid, transporting the resulting mixture from the bottom up through a layer of liquid with an adjustable level, preheating the moist material by passing through it the countercurrent gases obtained in the reaction zone, the supply of wet material to the reaction zone, its processing under elevated pressure and temperature to produce gases and solid product. The difference with this method is that the wet material is preheated before being fed into the reaction zone by passing through it the countercurrent gases obtained in the reaction zone. Moreover, in a device for thermal processing of organic carbon materials, including sequentially installed means for mixing the starting material with a liquid, is a transport container. fvjcpy. with a liquid installed at an angle to the horizontal plane and having means for transporting the material and means for adjusting the level of the liquid, a reaction chamber connected to the upper part with the upper part of the transport chamber and having means for removing the solid product and a nozzle for evacuating the gas in which The gas outlet is connected to the upper wall of the transport chamber above the liquid level. The reaction chamber is positioned in such a manner that its inlet opening is connected to the outlet opening of the transfer chamber for receiving the preheated starting material. The raw material is then heated in the reaction chamber to the desired elevated temperature for a period of time sufficient to effect its desired heat treatment, including the evaporation of at least some of the volatile substances forming the gas phase consisting of the condensing part and the substantially non-condensing part. t from the reaction chamber countercurrent to the direction of flow of the source material and during heat exchange contact with it, carried out a gradual condensation of condensing parts and accordant preheating of the source Material due to the release of latent heat of evaporation. The resulting condensed liquid drains from the starting material and mixes with the liquid in the lower part of the transfer chamber. The remaining non-condensing gaseous portion is discharged through a nozzle in the transport chamber, located above the working level of the liquid, and the outlet of the transport chamber. The gaseous reaction product from the reaction chamber is cooled to recover a significant portion of the heat by evaporating the liquid coming into contact with it, forming an additional condensing gas phase, which is passed through countercurrent to the starting material. Fig. 1 shows a device with a vertical reaction chamber; the section in Fig. 2 is a flow chart of the technological operations; Fig. 3 is an embodiment of a means for discharging a solid product. The device includes a storage bin 1, which is a means for mixing the starting material with a liquid. The hopper 1 is adapted to be filled with a specific carbon source material and has a flange 2 above the upper inlet end, which is closed and sealed with a solid flange 3. The lower part of the storage bin 1 is sealed by means of a flange 4 to the flange 5 connected to port b connected hole 7 with the lower end of the part inclined at an angle to the transport chamber 8. The transport chamber 8 has a circular cross-section and the same diameter along its entire length. Along the entire length of the transport chamber 8, a worm-type conveyor 9 or screw auger is installed. During rotation, it rests with its upper end on the end tip 10 bolted to the upper end of the transport chamber 8, and at its lower end is fixed by means of a support structure 11 and a flange 12, firmly bolted for tight connection to the flange 13 connected to the lower horse of the transport chamber 8. The central shaft 14 of the worm conveyor 9 is above the supporting structure 11 and connected by means of a clutch 15 to an electric motor m 16 with variable speed, to be able to carry out its rotation at a controlled speed.
    In the bunker 1, the pump 17 supplies water. The pump 17 operates interconnected with the flow control valve 18. The working fluid level 19 in the transport chamber 8 can be adjusted automatically or visually, for example, by linking a liquid level indicator (not shown) to the lower 20 and upper 21 drain holes located on the transport chamber 8, which makes it possible to note the minimum and maximum liquid levels, respectively. Flow control valve 18 operates in accordance with changes in the level of the working fluid in order to keep it substantially constant during the operation.
    The liquid introduced into the storage bin 1 in order to seal it and form a liquid paste with a certain organic starting material is usually water, but it may be another liquid that can evaporate and can be condensed under the conditions of temperatures and pressures used in device. Usually, the raw materials of the processed type contain different amounts of moisture and use.
    water only supplements the amount of water introduced into the source material itself, and also provides excellent heat transfer between the source material and the resulting product, achieving optimal recovery of the heat introduced into the system.
    The transfer chamber 8 is equipped with a gas outlet 22, located by the BbiLie of the maximum operating level of the liquid 19, in the transfer chamber. The port 22 is connected to the flow pressure control valve 23 and serves to discharge the condensable gases from the inside of the sports chamber 8 of the sport chamber 8. The connection between the transport chamber 8 and the inside of the pipe 22 is provided by a plurality of holes 24 formed in the wall of the transport chamber 8.
    0
    The source material, in addition to drying as it moves up, passes the working level of the liquid 19 in the transport chamber 8 and is also preheated
    5, a gas stream moving by a counter current and entering the upper part of the transport chamber 8 through a flange connection 25 attached to the upper end of the reaction chamber 26. The gas phase is a substantially non-condensable part consisting of various organic volatile substances released during heating
    5 of the carbonaceous material in the reactor, while the condensable phase is a liquid, such as water, formed during the final drying of the carbonaceous material in the reactor, as well as the liquid introduced through the pressure pump 27 to the bottom of the reaction chamber 26 to cool the carbonaceous material solid product.
    The reaction chamber 26 consists of a tubular portion 28 of a heat-resistant substance or metal, such as a high-temperature alloy of non-rusting steel, for example, which has a substantially uniform diameter along its entire length and is connected, for example, by welding with the upper flange 29 with the flange joint 25, and the bottom 5 A flange 30 with a flange 31 attached to the receiver 32 is heated there. The heating of the tubular part 28 and the carbonaceous raw material passing through it downwards is achieved by means of an electrical resistance winding 33 over which an insulating o material to minimize heat loss.
    The movement of carbon material down through the reaction chamber
    5 occurs under the influence of gravity and is controlled by a screw conveyor 34, which rotates from inside the pipe 35 and is driven through the gate 36 by an electric motor 37 at various speeds. Increasing or decreasing the speed of rotation of the screw conveyor 34 respectively changes the residence time of the carbonaceous material inside the hot zone of the reaction chamber 2.6 and correlates with the speed of rotation of the motor 16 connected to the screw conveyor 9 to provide the necessary heat treatment of the starting material. The level of carbonaceous material inside the reaction chamber 26 can be measured and / or adjusted with a suitable device 38 indicating the level and mounted on flange joint 25, which can be of any known type and commercially available. The reacted product, moving horizontally with the help of conveyor 34, is transported under the force of gravity into the bunker 39, which can be appropriately connected with one or several bunkers to carry out periodic removal of the reaction product from it. In accordance with an alternative option (FIG. 3), the product is continuously removed from the plenum chamber 26. The means for unloading is made in the form of an extruder 40 with a tapering extrusion orifice 41 tapering. In accordance with a specific alternative design (FIG. 3) the thermal reaction product entering into the extruder 40 is compressed to an insignificant porosity and extruded in the form of a rod or strip, which can be appropriately cut into pieces with a length suitable for further processing. The high pressure that the reaction product undergoes during the passage through the extrusion orifice 41 results in the formation of a self-supporting solution that prevents any pressure drop inside the system. In accordance with the arrangement, specific organic carbonaceous materials can be recycled in dry, wet or wet conditions at pressures from atmospheric to elevated to 3000 psi (211 kg / cm) and even higher pressure-dependent liquid components. and structural limitations of the device, and at temperatures of the order of several hundred degrees in order to realize the extraction function up to temperatures of the order of (1093c) and higher to achieve pyrolysis and essentially complete gasification of the starting material. The countercurrent of the gas phase flow generated in the reaction chamber relative to the input starting material is achieved by creating a pressure gradient with means for discharging the solid product in the receiver 32 by means of a nozzle 22 for exhausting gas. An example. Particles of a sub-bituminous coal, such as lignite, for example, as obtained during mining in the mine, are injected under pressure through a nutrient bunker and mixed with the fluid supplied by the pump 17. Typically, lignite of the type found in deposits located in the north central Vrratov anA, mainly in North and South Dakota and Wyoming, contains about 20–40% moisture and, therefore, there is no need for pre-production, since water is mixed with it to effect sealing. The pieces of lignite are continuously introduced into the lower part of the transport chamber 8 and are usually under a pressure of 1490 lb-in (104.7 kg / cm) and at a temperature of about (15). Wet particles of lignite rise up and they cross the phase boundary determined by the level of liquid 19. When passing above the working level of liquid 19, the lignite starting material is drained and preheated as a result of contact with the back-flow gas phase , as the material is lifted f by conveyor 9 to the upper part of the preheating zone of the transport chamber 8. Typically, the pressure in the preheating zone is 1490 psi (104.7 kg / cm), and the temperature vyye travel immediately the working fluid level is approximately (38 ° C). The voids in the preheating zone are filled with a gas phase that is adjacent to the level of the working fluid 19 and consists essentially of non-condensable gases generated in the reaction zone of the reaction chamber 26. The gas phase in the area of the preheating zone, adjacent to and directly above the level of the working fluid 19, represents It is a mixture of non-condensable gases and steam, and the partial pressure of the steam is in equilibrium with the temperature in the reaction chamber 26 at that particular location. With a further rise up of the lignite load, further preheating occurs during condensation of condensing steam in a countercurrent gas phase from the higher pressure section in the upper part of the transport chamber 8 to the lower pressure region adjacent to the gas outlet. The average pressure in the upper part of the preheating zone is approximately 1495 psi (105.0 kg / cm), and the gas phase composition gradually changes as it moves down to the nozzle 2-2 to allow the gas to escape as the vapor condenses on the surface. Double upward cold starting material. The pressure gradient required for the gas pressure of the countercurrent and helium particles is maintained by controlling the pressure at the gas outlet and the temperature of the receiver 32 for the solid product. In this particular example, the pressure in the nozzle 22 is set to 1490 psi (104.7 kg / cm), the temperature of the product in receiver 32 must be maintained above 598 ° L () by monitoring the amount of quenched injected water. At 598 F (314 ° C), the saturated vapor pressure equals 1500 psi (105.5 kg / cm2) and the pressure difference between the product discharge opening and the gas outlet opening is 10 psi (0.7 kg / cm). The actual pressure difference at any particular moment is a function of the gas flow rate and the resistance to the passage of the gas stream through a layer of particles. As long as the bunker 39 for the product and all adjacent surfaces are maintained at a temperature above the equilibrium temperature of the saturated bar at a system pressure (598 Fr 1500 psi (at 105.5 kg / cm), the pressure difference can be easily monitored. The vapor generated by the receiver 3 for the solid product will become superheated as it rises up through the reaction chamber 26 and is diluted with non-condensing gases formed in the hot zone. These hot gases are cooled due to heat exchange with the lump moving down because the gas continuously moves to the nozzle 22 for venting, the gas becomes colder due to the loss of a significant amount of heat until at the same point of the preheating zone the temperature reaches the equilibrium temperature for the saturated steam with partial vapor pressure in the gas stream. From this point to the nozzle 22, the composition of the passing gas stream gradually changes as the steam gradually condenses on the colder lignite. In this preheating region, the pressure gradient prevents non-condensing gases from flowing backwards, resulting in a concentrated gradient of non-condensing gases that reaches 100% of non-condensing gases at the cold end of the preheating zone, a mixture of gas and steam in the heating zone and essentially 100% condensing gases or steam in the cold zone of the system. When transferring preheated lignite from the upper end of the zone, it is preferable to provide some amount of empty space in order to adapt to improved control of the flow rate of solid particles in the reaction chamber 26. When entering the upper end of the reaction chamber 26, the solid particles are heated to the desired elevated temperature and the amount of heat required. proportional to the heat loss through the walls of the reaction chamber 26 and that which is released from the system with a refined coal product and with gases discharged from the system. The pressure in the reaction chamber 26 is about 1495 psi (105.2 kg / cm) and the temperature is about 950 F (510 ° C). The gas phase in the reaction zone is a mixture of essentially non-condensable gases in combination with condensing gases as superheated steam. As the reaction zone passes downward, the refined lignite coal product is cooled by injecting water under a pressure of 150 psi (105.5 kg / cm) or higher by pump 27, which is corrected at a rate sufficient to maintain the pressure in the reaction chamber 26 and receiver 32 of about l500 pounds per inch (105.5 kg / cm). The equilibrium temperature of the saturated steam obtained in the cooling zone is (314 ° C) and the cooled product must have a corresponding temperature. After that, the cooled product is transported by some kind of conveyor 34 to bunker 39 and pressurize 1500 psi (10.05 kg / cm D for the same price)
    Thus, a dynamic concentrated gas phase gradient between the hot and cold ends of the apparatus is provided, as a result of which essentially all the released heat is recovered due to condensation of the condensable phase by preheating the introduced starting material.
    iO
    1
    权利要求:
    Claims (2)
    [1]
    1. The method of heat treatment of organic carbon materials, including mixing the source material with a liquid, transporting the resulting mixture from bottom to top through a liquid layer with an adjustable level, supplying wet material to the reaction zone, processing it at elevated pressure and temperature to produce gases and a solid product, removal gases and a solid product, characterized in that, in order to increase efficiency, the wet material is preheated before being fed into the reaction aeon by passing through it a counterflow of gases obtained in the reaction zone.
    [2]
    2. A device for thermal processing of organic carbon materials, including sequentially installed means for mixing the starting material with liquid, a transport chamber with liquid mounted at an angle to the horizontal plane and having means for conveying the material and means for controlling the liquid level, a reaction chamber connected to the top part with the upper part of the transport chamber and having means for discharging a solid product and a pipe for discharging gas, characterized in that in order to increase efficiency, a degassing pipe is connected to the top wall of the transport chamber above the liquid level.
    类似技术:
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    SU1085509A3|1984-04-07|Method and apparatus for thermal treatment of organic carbonaceuos materials
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    同族专利:
    公开号 | 公开日
    SE7809462L|1979-03-13|
    ES473280A1|1979-04-01|
    DE2839663C2|1986-07-31|
    AT372104B|1983-09-12|
    IL55377D0|1978-10-31|
    AU3975178A|1980-03-20|
    FI782756A|1979-03-13|
    DE2839663A1|1979-03-22|
    DD138778A5|1979-11-21|
    GB2004988A|1979-04-11|
    GB2004988B|1982-03-10|
    FR2402475B1|1983-07-01|
    FI69313B|1985-09-30|
    JPS5944347B2|1984-10-29|
    SE440790B|1985-08-19|
    JPS5456602A|1979-05-07|
    AU515318B2|1981-03-26|
    ZA784636B|1980-03-26|
    FR2402475A1|1979-04-06|
    US4126519A|1978-11-21|
    BR7805909A|1979-05-02|
    ATA658178A|1983-01-15|
    CA1109821A|1981-09-29|
    PL209538A1|1979-07-16|
    FI69313C|1986-01-10|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/832,363|US4126519A|1977-09-12|1977-09-12|Apparatus and method for thermal treatment of organic carbonaceous material|
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