• 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:
    This invention relates to a process for the production of synthesis gas by the incomplete oxidation of coal suspended in water at elevated pressure and a temperature of 1000-1 BOO s and allows an increase in the degree of carbon conversion. 3-20% of the required total amount of oxygen or 1-19% of synthesis gas oxygen is fed through the central channel, through the intermediate annular channel - a stream of aqueous coal slurry and through the outer annular channel an additional oxygen-containing stream, with the coal slurry stream being fed at a rate of 1 -25 m / s at an angle relative to the direction of flow of the oxygen-containing stream supplied through the central channel, and oxygen-containing flows fall at a speed of 50-300 m / s at an angle relative to the direction of flow of the aqueous stream enzii arc. 1 hp f-ly, 1 ill., 1 tab. O) with about with.
    公开号:SU1309913A3
    申请号:SU833592359
    申请日:1983-05-19
    公开日:1987-05-07
    发明作者:Матерне Винфрид；Шлепер Бернхард；Герхардус Ульрих；Хиббель Йозеф；Лидер Бернхард；Шеве Хайнрих；Шмидт Фолькмар
    申请人:Рурхеми Аг (Фирма)；
    IPC主号:
    专利说明:

    eleven
    The invention relates to methods for producing synthesis gas.
    The aim of the invention is to increase the conversion of coal.
    The drawing shows an apparatus for carrying out a method for producing synthesis gas by partially oxidizing coal suspended in water with oxygen-containing gas.
    YuOO-GbOO C under pressure of 10-200 bars
    The device contains a reactor 1, in the upper part of which a means (a burner) is installed for introducing an aqueous suspension of coal and oxygen. The burner consists of an outer pipe 2 for the supply of a stream of pure oxygen or an oxygen-containing gas mixture, a middle pipe 3 for supplying a suspension of coal in water, and an internal (central pipe 4 for supplying oxygen-containing gas.
    The outer pipe 2 has a conical narrowing — a nozzle 5. At the end of the middle pipe 3, a conical narrowing is made, a nozzle 6, and the end of the central inner pipe 4 is also made in the form of a conical narrowing — a nozzle 7; The angle of the narrowing and the distance of the three nozzles The angle of the three streams is relative to each other and influences the process in the reaction zone 8. The burner nozzles are made of thermal and wear resistant material.
    In order to reduce the thermal load of the burner end, the outer tube 2 is provided with a cooling element 9, through which coolant (water or steam) is passed. The flange 10 serves to secure the burner to the reactor 1.
    The cooling element 9 has an inlet and an outlet in the flange 10; it is structurally designed so that the cooling section of the channel 11 is in a conical narrowing - cone 5.
    The flanged pipe 12 is attached to the outer pipe 2 and is squeezed to supply an external gas stream. An internal gas stream is fed into the middle pipe 3 through a flange 13, which is flanged with a flange, and an internal gas stream is fed into the internal pipe 4 through a pipe 14 fitted with a flange,
    The movement of the pipe 2 relative to the pipe 3 in order to change the flow area of the nozzle opening and increase the flow rate is carried









    five
    0
    0

    35
    0
    five
    blowing way. Above the nozzle 12 there is a flange 15 with a fixed retaining ring 16 and a threaded nut 17 connected to a worm gear 18, which is driven by a motor 19 connected by a chain gear with a worm gear 20.
    The control shtutser 21 is designed to test the sealing rings 22. The fitting 23 serves to connect a shut-off chamber (not shown) that prevents the release of pressurized oxygen or an oxygen-containing gas mixture.
    In addition, a cooling device is arranged at the lower end of the flange 15, consisting of a cooling channel 24 with conduits 25 and 26 for supplying and discharging the cooling agent.
    The pipe 4 is moved relative to the pipe 3 to change the flow rate of the reaction mixture using the same mechanism described on the flange 27 through the stationary 1st retaining ring 28 with a screw nut 29 connected to a worm gear 30, which is driven by a chain transmission engine 31 with a worm shaft 32.
    Thus, it is possible to change the flow rate of the reaction mixture to increase the degree of conversion.
    The device works as follows.
    Through the middle pipe 3, a suspension of coal in water is fed to the reactor under a pressure of 10–200 bar, at a speed of 1–25 m / s, and through the central and outer pipes, gas flows into the reaction zone at a speed of 50–300 m / s. . Concentric tubes through which they pass separately, but
    at the same time, suspension angle
    both gas streams and in water have on their
    five
    facing the reaction zone end conical constriction.
    For a conical narrowing of the internal gas flow, a relatively small angle of 0-15 ° relative to the central axis of the burner was selected, while the angle of supply of the internal gas flow of coal suspension in water should be 5 g40 relative to the central axis of the burner, and the angle of feed 3130
    Along the gas flow is also relative to the central axis of the burner 10-85 °.
    Due to the appropriate combination of conical constrictions, the direction of flow of the coal suspension in water forms, together with the direction of flow of the internal gas flow, an angle of 5-30 °, and the direction of flow of the external gas flow forms an angle of 5-50 ° with the direction of flow of the suspension of coal in water. As a consequence, the suspension stream near the end of the conical narrowing expands with an internal gas stream. Thus, the slurry stream is horizontally deflected and does not pass through the free fall reaction zone. As a result, the average residence time of the individual coal and water droplets is increased, which leads to a better conversion.
    At the same time, the external gas flow hits the slurry stream expanded by the internal gas flow and causes additional mixing of the gas with the suspension to form a zone of uniform distribution of gas or oxygen and small droplets of the suspension, which is an essential prerequisite for achieving a high degree of conversion, suspension. This is additionally supported by varying the rate at which the coal slurry enters the water and the gas flows. In addition, it is possible to supply the gas stream to the reaction zone at a faster rate than the external gas stream, and vice versa.
    As confirmed by the experiments, the reaction zone 8 is formed at the mouth of the burner.
    In a coal gasification device, the used amount of coal suspension in water and gas or oxygen can be consistent with increasing demand or decreasing demand, but stopping the device should be avoided. Even a short-term termination of work leads to unacceptable cooling of the reactor, resulting in difficulties in the implementation of the new gasification process, since the lining must have an appropriate temperature, providing chemical conversion of water and coal. This is achieved by continuously increasing the reduction of the free outflow openings of the coal suspension in water and the external gas flow.
    34
    The middle tube, through which the coal suspension in water is fed through the annular space formed together with the inner tube, is not rigidly connected to the inner tube, but so that the inner tube can be moved in the direction of the centric axis relative to the middle tube.
    Regardless of the movement of the inner tube, the middle tube can also be continuously moved relative to the outer, fixed tube.
    If the middle pipe is moved in the direction of its outlet orifice, the annular gap between the inner side of the outer pipe and the outer side of the middle pipe begins to decrease evenly. Since the magnitude of this annular gap affects the amount of external gas flow, i.e. reducing the annular gap leads to a decrease in gas consumption, and increasing the annular gap to an increase in the amount of gas, the gasification process can be appropriately coordinated with the requirements in each case without stopping the gasification process. The same applies, irrespective of the change in the outer annular gap, to the annular gap through which the coal slurry exits in water. Moving the inner tube in the direction of its outlet, i.e. parallel to the central axis of the burner, helps to reduce the annular gap formed between the inner side of the middle pipe and the outer side of the inner pipe. Moving the inner tube back leads to an increase in the free annular space and thus to an increased consumption of coal slurry in
    water.
    The required, if necessary, change in the amount of gas supplied through the inner tube can be made by increasing or decreasing the gas pressure. Increasing the pressure: Neither gas contributes (at a constant pressure during the gasification process) to a greater amount of gas, and a decrease in gas pressure to a decrease in the amount of internal gas flow. Thus, it is possible to coordinate the gasification process with the required amount of synthesis gas without shutting down the installation
    15
    Example 1 To a reaction zone in which the temperature is maintained at 145 ° C and a pressure of 20 bar, 3070 kg / h of aqueous coal suspensions containing 65.5% by weight of solid matter and 5 to 48.3% by weight of carbon and 1290 oxygen are fed. The total amount of oxygen is divided into two streams, and the gas stream supplied through the center of the coal stream contains 20% of the total amount of oxygen.
    The resulting synthesis gas contains,%: CO 48; H 37; WITH 15.
    The degree of carbon conversion in terms of carbon source 98.5%.
    Example 2. Example 1 is repeated, with the difference that the gas flow supplied in the center contains 3% of the total oxygen and the concentric flow of the gas flow - 97% of the total oxygen, both of which are fed at a speed of 130 m / s. . A synthesis gas is obtained that contains,% by volume: C04b, 5; H 7; COj 16.5. The degree of conversion of coal, in terms of source carbon 97%.
    Example 6: Example 1 is repeated. The only difference is that the gas supplied in the center contains 2% of the total amount of oxygen, and the gas flow concentrically is 98% of the total amount of oxygen. The degree of conversion is 93.9%.
    13099136
    Example 4. Example 1 is repeated with the difference that 21% of the total amount of oxygen is supplied through the central channel. The degree of conversion of 98.5%.
    EXAMPLE 5 Example 1 is repeated, with the difference that the weight flow of synthesis gas is injected into the oxygen feed through the center. The resulting synthesis gas contains,%: CO 46, 7; H537; COj 16.3. The degree of carbon conversion in terms of carbon source 97.4%.
    Example 6. Example 1 is repeated, with the difference that 19% by weight of synthesis gas is introduced into the gas flow fed to the center, thus obtaining synthesis gas containing CO 48.2; Hj 37; CO 14.8. The degree of carbon conversion in terms of the original carbon is 98.7%.
    Example 7. With the introduction of 0.8 wt.% Synthesis gas, the conversion rate did not increase as compared with Example 5, i.e. does not exceed 97%, and when introduced in an amount of 20% by weight, the degree of carbon conversion decreases to 98.4%.
    Example 8. Example I is repeated at different speeds and angles of coal and gas supply.
    Results: the experiments are shown in the table,
    thirty
     Regarding the direction of flow of the oxygen-containing stream supplied
    in the center of the flow of coal. Regarding the flow direction of the coal.
    7130
    When conducting experiments on a known method, the degree of conversion of 85 - 88.4%, and according to the proposed - 93.9-99.5%.
    权利要求:
    Claims (2)
    [1]
    1. A method of producing synthesis gas by feeding an oxygen-containing stream through a central burner channel, an aqueous suspension of coal through an intermediate annular channel — a stream of coal slurry and an additional oxygen-containing stream through an external annular Lacal;
    25 m / s at an angle relative to the direction of flow of the oxygen-containing stream supplied through the central channel, and oxygen-containing flows at a speed of 50-300 m / s at an angle relative to the direction of flow of the coal stream, characterized in that, in order to increase the degree of carbon conversion, through the central channel serves 3-20% of the required total amount of oxygen.
    [2]
    2. The method of pop. 1, which differs from the fact that a stream containing 1–19% of synthesis gas oxygen is fed through the central channel.
    K23 32
    Compiled by I.Popov Editor O. Yurkovetska Tehred M. Hodanich.
    Order 1809/58 Circulation 464 Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Production and printing company, Uzhgorod, st. Project, 4
    Proofreader M.Sharoshi
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3219316A|DE3219316A1|1982-05-22|1982-05-22|METHOD AND DEVICE FOR PRODUCING SYNTHESIS GAS BY PARTIAL OXIDATION OF COAL-WATER SUSPENSIONS|
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