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    • 专利摘要:
    Zur Herstellung von Acetylen und Synthese- oder Reduktionsgas aus Kohle mittels eines Lichtbogen- oder Plasmaverfahrens pyrolysiert man pulverförmig aufbereitete Kohle in einem ersten Lichtbogenreaktor bei einer Energiedichte von 1 bis 5 kWh/Nm3, einer Verweilzeit von 0,5 bis 10 msec und Temperaturen von mindestens 1500°C in der Weise, daß die aus der Kohle gewonnenen, gasförmigen Verbindungen das 1,8fache der sogenannten «Flüchtigen» der Kohle nicht übersteigen. Der nach dem Quenchen zurückbleibende Koks wird dann einem zweiten Lichtbogenreaktor zugeführt, in dem der Koks mittels eines Vergasungsmittels und Aufheizen mittels eines Lichtbogen- oder Plasmaverfahrens bei einer Verweilzeit von 1 bis 15 sec und einer Temperatur von mindestens 800°C zu Synthese- oder Reduktionsgas umgesetzt wird. Der Gasstrom aus der Pyrolysezone wird gereinigt und aus diesem das Acetylen durch selektive Lösungsmittel gewonnen. Das Gas aus der Vergasungsstufe wird gegebenenfalls abgekühlt und gereinigt.
    公开号:SU1531849A3
    申请号:SU843784984
    申请日:1984-08-24
    公开日:1989-12-23
    发明作者:Мюллер Рихард；Керкер Лотар；Пейкерт Корнелиус
    申请人:Хемише Верке Хюльс Аг (Фирма)；
    IPC主号:
    专利说明:

    315
    are heated to an average temperature of 3% and 3 are pyrolyzed for 2 m. The resulting gas-coke mixture is cooled by adding water to a temperature, then the coke in the cyclone is separated and the gas is fed to the purification by washing with water or lye. The amount of gas produced is 45 kg / h, which corresponds to 1.5 times the amount of volatile components in the starting coal. The output of acetylene in terms of the original coal is 32%, and the specific energy consumption is 11.3 kWh / kg of acetylene.
    The degree of use of coal is 45%.
    Separated from gas, coke with a temperature of 150 ° C, containing 9.8% of volatile components, is fed from the top into a cylindrical reactor equipped with a lining using a mixture of 25% water vapor and 75% hydrogen. At the same time, a plasma jet of hydrogen having an energy density of 3.0 kWh / nm is supplied to the reactor. This jet is created in a 300 kW electric arc reactor. In addition, water vapor is fed from above into the reactor so that, in terms of carbon content in coke, the molar ratio of 0: C is maintained equal to. Gasification is carried out at an average temperature of 1300 ° C for 6 s.
    A portion of the slag is obtained in liquid form at the bottom of the reactor, and the gas is drained from the side at the end of the reactor, passed through a heat exchanger and is cooled in the Venturi scrubber to. At the same time, the soot is washed out, so that there is no carbon in the exhaust gas. Samples of running water are taken and the solid carbon content is determined.
    By the amount of water and carbon content, you can determine the degree of gasification (97%). The output of synthesis gas (CO + H) 3.6 nm / kg of coke.
    The overall utilization of coal is 98.3%.
    Example 2. A 360-kW single-stage electric arc furnace operating on a mixture of 80% hydrogen, 19% carbon monoxide and 1% methane as part of the gas flow gas from the gasification stage, with an energy density of 2.8 kWh / nm and 0.5 bar pressure serves finely divided coal containing volatile components
    five
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    25% in the amount of 120 kg / h (excluding water and 3osu) using gas of the same composition as the plasma gas, and subjected to pyrolysis at an average temperature of 2200 ° C for 2 m-s. The resulting gas-coke mixture is cooled to 600 ° C with water and then brought to a heat recovery boiler. Coke and gas are separated as in Example 1. The separated coke contains 9.8% volatile components. Gas outlet, i.e. coal utilization rate, 42%, i.e. 1.68-fold volatile components ang. The yield of acetylene in terms of the initial coal is 27% at a specific energy consumption of 11.1 kW / h of kg of acetylene. Further work as in example 1. At the same time the degree of gasification is 92%. and the yield of synthesis gas is 3.4 nm / kg.
    The overall utilization of coal is 96%.
     Example 3. Example 1 is repeated with the only difference that a plasma jet fed into the gasifier is generated in a 300 kW electric arc reactor from a gas mixture containing,% by volume: hydrogen 60, water vapor 25-, carbon dioxide 10, carbon monoxide 5. The energy density of 3.2 kWh / nm .. At this, the ratio of 0: C, equal to 1: 2. the process is carried out at an average temperature of 1350 ° C for 5 s. The degree of gasification is 95%, which corresponds to a synthesis gas output of 3.5 coke.
    The overall utilization of coal is 98%.
    Example 4. Example 1 is repeated with the difference that the pyrolysis is carried out in a single-stage electric arc furnace with a power of 300 kW with a dense energy of 1 kW / nm, an average temperature of 1500 s and a pressure of 0.1 bar for 10 m-s using coal containing 39.8% volatile components.
    In this case, the gas output, i.e. coal utilization rate 31.8%. which corresponds to 0.8 times the amount of volatile components of coal. The output of acetylene in terms of the original coal is 23.1% with a specific energy consumption of 13 kWh / kg acetylene.
    Separated from gas, coke, containing 5.8% of volatile components, is gasified at an energy density of a plasma jet of hydrogen equal to 3.9 kWh / nm and an average temperature
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    , for a period of 1 s. The degree of gasification is 97%, and the yield of synthesis gas is 3.6 coke.
    The overall utilization of coal is 98%.
    Example 5. A 360 kW electric arc furnace operating on hydrogen at a pressure of 1.2 bar and an energy density of 5 kWh / s serves 120 kg / h (excluding water | and h0 / g) fine coal (90%, - 150 µm), containing 27.3% of volatile components, with help (and a hydrogen stream under a load of 20 kg / kg gas. Pyrolysis is carried out at / medium temperature for 0.5 second, after which the reaction is stopped by cooling with water.
    Gas outlet, i.e. degree of use of coal, 49.1%, which corresponds to 1, 8 times the amount of volatile components of the original coal. The yield of acetylene in terms of the original coal is 27.3%, which corresponds to the specific energy consumption of 11.0 kNt h / kg of acetylene.
    60 kg (excluding water and ash) of coke with a volatile content of 5.3%, separated from the pyrolysis gas products, are fed to a reactor equipped with a lining using a gas mixture consisting of 80% hydrogen, 19% carbon dioxide and 1 % methane. The reaction mixture is subjected to a plasma jet with the same composition as the carrier gas, having an energy density of 2.3 kWh / nm (the jet is created in an arc of 240 kW kW). By adding water vapor, the P: C ratio is adjusted to 1.15.
    Gasification is carried out at an average temperature of 800 ° C for 15 seconds. At that, the degree of gasification is 92%, and the yield of synthesis gas is 3.4 nm / kg of coke.
    The overall utilization of coal is 95%.
    Example 6. Example 5 is repeated, with the difference that 140 kg / h (excluding water and ash) of hard coal, containing 16.1% of volatile components, are used. In this case, pyrolysis is stopped after the formation of gas in the amount of 28.2%, which corresponds to 1.75 times the amount of volatile components in the starting coal.
    Thus the degree of utilization of coal is 28.2%.
    96
    The output of acetylene in terms of the original coal is 22.2% with a specific energy consumption of 12.7 kWh / kg acetylene.
    Coke with a volatile content of 6.7%, separated from the pyrolysis gas products, is gasified under the conditions of Example 1. When
    This degree of gasification 93%, and the yield of synthesis gas 3.4 nm / kg of coke.
    The overall utilization of coal is 95.7%.
    Example 7. Repeat example.
    1 with the difference that they use
    104 kg of finely crushed and dried drilling coal containing 4% ash and 49% volatile components. Amount of gas generated 78.4 kg / h
    which corresponds to 1, 6 times the amount of volatile components in the starting coal. Thus, the degree of utilization of coal is 78.4%. The output of acetylene in terms of the original coal
    29.9%, and the specific energy consumption of 12.5 kWh / kg acetylene.
    Coke separated from gas, containing 7.3% of volatile components, with a temperature of 150 C is fed from above into the supply
    lined with a cylindrical reactor using a mixture of 25% water vapor and 75% hydrogen. The gasification is carried out as described in example 1.
    By the amount of water and content
    carbon can determine the degree
    gasification (91%). Synthesis gas synthesis gas (CO + Hj) 3.4 nm / kg coke.
    Total coal utilization
    98.4%.
    Example 8 (by a known method). Example 7 is repeated with the difference that the pyrolysis is carried out at a temperature of 4200 K and an energy density of 6 kWh / nm for 1 m-s. At the same time, the amount of produced gas is 68.3 kg / h, which corresponds to 1, 4 times the number of components in the starting angle.
    Thus, the degree of utilization of coal is 68.3%. The output of acetylene is in terms of the original coal, and the effective energy consumption is 23.9 kWh / kg of cetylene.
    Separated from gas, coke with 2.1% volatile components, with a temperature of 150 ° C is fed from above into a cylindrical rector equipped with lining using a mixture of 25% solids
    th steam and 75% hydrogen. The gasification is carried out as described in example 1.
    By the amount of water and carbon content, you can determine the degree of gasification (70%). The output of synthesis gas (CO + H) 2,6 nm / kg KOKcaji
    Thus, the degree of utilization of coal is only 89%.
    Comparison of the results of examples 1 with the results of comparative experience 8 indicates the achievement of the goal of the proposed method. In addition, the efficiency of the proposed method is also due to the fact that the specific energy consumption is much lower. , P. and M e R 9. The example is repeated with the difference that the pyrolysis is carried out for 13 ms. You get 60 kg / h of gas, which corresponds to 2 times the amount of volatile components of the original coal.
    Thus, the degree of utilization of coal is 60%.
    The yield of acetate in terms of the original coal is 27%, and the specific energy consumption is 13.3 kWh / kg acetylene.
    By gasifying coke separated from gaseous pyrolysis products containing 3.3% of volatile components, in the conditions of example 1, the following results are obtained.
    - The degree of gasification is 70%, and the yield of synthesis gas is 2.6 nm / kg of coke. Overall use rate of 88%.
    Example 10. Example 1 is repeated with the difference that the pyrolysis is carried out for 9 M C with a plasma jet energy density of 6 kWh / nm. You get 57.7 kg / h of gas, which corresponds to 1.9-fold the amount of volatile components of the original coal. The output of acetylene in terms of the original coal is 26.3%, the specific energy consumption is 13.7 kWh / kg of acetylene, and coal utilization rate is 57.7%.
    When gasifying coke separated from gaseous pyrolysis products containing 2.9% volatile components under the conditions of Example 1, the following results are obtained.
    The degree of gasification is 73%. and the yield of synthesis gas is 2.7 nm / kg of coke. Total degree (T) of coal is 87%.
    The results of Example 1 and Comparative Examples 9, 10 are equivalent. that when pr-ezde0
    five
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    five
    Research Institute of pyrolysis before the formation of gaseous compounds in an amount greater than 1.8 times the amount of volatile components of the original coal, the yield of acetylene decreases from 32 to 27 and 26.3%, respectively, with an increase in specific energy consumption from 11.3 to 13.3 and 13 , 7 kW, h / kg of acetylene, respectively, and, in addition, the degree of gasification decreases from 97 to 70 and 73%, respectively, which means a 25-28% decrease in the synthesis gas yield (from 3.6 to 2.6-2 , 7 nm / kg coke). The overall utilization of coal is significantly reduced.
    Example 11. Example 4 is repeated with the difference that the pyrolysis is carried out in a 250 kW electric arc furnace. At the same time, the energy density is 0.8 kWh / nm and the average temperature decreases to 1400 ° C. Gas is produced in co: 1 quality of 25.3%, which corresponds to 0.6 times the amount of volatile components of the original coal.
    The output of acetylene in terms of the original coal is 12.9% with a specific energy consumption of 19.4 kWh / kg acetylene. Thus, the degree of utilization of coal is 25.3%.
    When gasifying coke separated from gaseous pyrolysis products containing 23.9% of volatile components, the following results are obtained under the conditions of Example 4.
    CTerietii, ha and () concentration, 78%, and the yield of synthesis gas is 2.8 nm / kg of coke. The amount of carbon used is 82%.
    Comparison of the results of Example A and Comparative Example 11 shows that when pyrolysis is carried out before the formation of gaseous compounds in an amount less than 0.8 times the amount of volatile components of the ISCHOD01-0 coal, the yield of acetylene decreases from 23.1 to 12.9 % with an increase in specific energy consumption from 13.7 to 19.4 kWh / kg of acetylene, and the synthesis gas output decreases from 3.6 to 2.8 coke while reducing the degree of gasification from 97 to 78%.
    The overall degree of coal utilization is significantly reduced,
    PRI me R 12. CHS ptor ntg example p I with a roil difference G ;, tgs g PI | and 11 ;, P1, py carry out PRI and I t; qonvrr
    16 s The degree of gasification 577 ,, and the output of synthesis gas is 2 coke.
    Example 13. Example 1 is repeated with the difference that gasification is carried out at PHC for 0.8 s. The degree of gasification is 67%, the yield of synthesis gas is 2.4 nm / kg of coke.
    Data on the amount and composition of acetylene-containing gas and synthesis gas are summarized in the table.
    Comparison of the results of gasification in examples 1-7 with the results of gasification in comparative examples 12 and 13 indicates the materiality of the proposed limits of the gasification process, since if they are not observed, the results of gasification are unsatisfactory.
    p and
    ten
    53184910
    权利要求:
    Claims (1)
    [1]
    Claims A method for producing acetylene and syn-gas by pyrolisation in a stream | carrier gas in an electric arc reactor, cooling of pyrolysis products and subsequent separation of an acetylene-containing gas stream, characterized in that, in order to increase the efficiency of the process due to more complete and efficient use of raw materials, pyrolysis is carried out. at an energy density of 1–5 kWh / nm and a temperature of 1,500–2,600 ° C for 0.5–10 ms to form gaseous compounds in an amount of 0.8–1.8 times the volatile components of coal, and the pyrolysis residue containing 5.3–12.8% of volatile components is gasified using 1 plasma technology in the presence of a gasification agent at 800–1700 s for 1–15 s.
    15
    20
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19833330750|DE3330750A1|1983-08-26|1983-08-26|METHOD FOR GENERATING ACETYLENE AND SYNTHESIS OR REDUCING GAS FROM COAL IN AN ARC PROCESS|
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