• 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:
    The invention relates to the recovery of chemicals from waste liquor from wood pulp process, primarily black liquor, while utilizing energy liberated. Controlled total vaporization of the pulp waste liquor at high temperature and low oxygen potential is achieved by the external supply of energy. During the subsequent condensation and separation a melt or water solution is obtained which, without causticizing, can be used for the preparation of white liquor, and also an energy rich gas and mainly free from sulphur, consisting primarily of carbon monoxide and hydrogen.
    公开号:SU1443810A3
    申请号:SU843731146
    申请日:1984-04-17
    公开日:1988-12-07
    发明作者:Сантен Свен；Бернхард Рагнар；Мальмеблад Свен-Эрик
    申请人:Скф Стил Инджиниринг Аб (Фирма)；
    IPC主号:
    专利说明:

    O5 O)
    ,
    The invention relates to the pulp and paper industry.
    The purpose of the invention is to simplify the method and allow individual control of temperature and oxygen potential during the processing of the liquor.
    The essence of the invention is that the spent liquor from the cellulose production is introduced into the reaction zone of the reactor with simultaneous supply of external thermal energy, regardless of combustion, while the temperature and oxygen potential are individually and carefully controlled using an adjustable supply of this thermal energy and possible addition of carbon-containing material and / or oxygen-containing gas, and. the resulting product is cooled or allowed to cool in a cooling zone located in said reactor. The inorganic components are excreted in the form of a melt or an aqueous solution, the organic part is removed in the form of a gas consisting mainly of hydrogen and carbon monoxide.
    The external supply of energy to the reaction zone of the reactor leads to a high temperature with a low oxygen potential and the Na thus obtained is contained mainly in the form of a monatomic gas. Via . carefully controlled oxygen potential and temperature, preferably provided by the use of high calorific gas heated in a plasma generator to supply external thermal energy sodium hydroxide and sodium sulfide are the main components produced by cooling, while the formation of sodium carbonate is slow is.
    In addition, temperature control provides valuable gas containing almost only hydrogen and carbon monoxide, which can be used to produce steam as a synthesis gas, and the like.
    Since the danger of a melt-water explosion in the proposed method is eliminated, the vapor pressure can be increased during the steam generation process and most of the thermal energy can be used as electrical energy in the turbine. :
    25
    thirty
    5 10 15 20
    35 , 10 45
    , 50
    j th
    The proposed method is carried out in a reactor containing reaction and cooling zones with supplying them with pipelines for supplying waste liquor, as well as pipelines for possible supply of additional material, such as carbon-containing material, oxygen-containing gas and the like, as well as a source of external heat, wherein the cooling zone is provided with a lower outlet nozzle for withdrawing inorganic components in the form of a melt or an aqueous solution, and an upper venting nozzle for withdrawing the produced gas. A plasma generator is used as an external source of tallow energy.
    FIG. I depicts a reactor for carrying out the proposed process; in fig. 2 is a flow chart for the production of chemicals from spent liquor from sulphate pulp production; in fig. 3 - modification of the technological scheme.
    The reactor (Fig. 1) consists of reaction 1 and cooling 2 zones. Partial evaporation of the spent liquor and decomposition is carried out in the reaction zone with the supply of extra-thermal energy, regardless of combustion using high-calorific gas heated using a plasma generator 3. The heated gas is removed through pipe 4.
    The energy supply is regulated so that the temperature in the combustion chamber is maintained in the range of 1000 - 1300 ° C. The spent liquor is introduced through the inlet 5. Additional inlet pipes 6 are provided for the carbon-containing material and / or oxygen-containing gas in order to regulate the oxygen potential and temperature in the reaction zone, as well as to control the partial pressure of carbon dioxide.
    Using a plasma generator to supply external energy allows complete evaporation of liquor. In the resulting equilibrium mixture, sodium is thus approximately 99% in the form of a monatomic gas.
    From the reaction zone, the resulting product passes into cooling zone 2, where the temperature is maintained at
    range is 600-900 ° C. Thus, a series of condensed sodium compounds is formed by the following reactions: 2Ma + 2HjO 2NaOlI + Hg
     + CO.
    Na, rc, + I O
    2NaOH + NajS 2H-jO
    By controlling the ratios of the partial pressure and the CO / CO reaction can be adjusted to minimize the sodium carbonate content in the melt.
    The melt containing sodium hydroxide, sodium sulfide and a small amount of sodium carbonate is extracted from cooling zone 2 through outlet 7. Depending on cooling, the resulting inorganic product can also be removed as an aqueous solution, in which case the sulfide is in the form of an acidic sodium sulphide.
    High-calorie gas containing mainly hydrogen and carbon monoxide is removed through a gas outlet pipe 8 in order to use it for generating energy in a steam boiler or as synthesis gas and the like.
    Example 1 (Fig. 2). Take the cooking waste liquor with a dry vernal content (MW) of 67%, having the following elemental composition,% C 35; H 4; Na 19; S 5; and O 37.
    1800 kWh per ton of SV supply through the plasma generator, as an external energy source, thus driving the liquor to evaporate completely. The temperature in the reaction zone is maintained at approximately 1200 ° C, and the temperature in the cooling zone in the plasma reactor is. pe - approximately 800 ° C, after which the inorganic substance is separated in liquid form. A reaction takes place between the resulting sulfur-hydrogen and the melt in the cooling zone, resulting in an exceptionally low sulfur content in the exhaust gas. In the exhaust gas, reduced to normal levels in pressure and temperature, contains the following amount of CB thick liquor (in terms of ton), COi 90; CO 558; 333; At 680; NgO, 3; Na 0.2.
    In terms of tonnes of dry liquor, the resulting melt contains, kg: 44; NaOII 17; 120
    The resulting melt contains only about 13% sodium carbonate, which can be compared with the product obtained after the known causticization, which contains approximately 25% sodium carbonate. The resulting product can be used directly to produce sulphate cooking liquor without caustification stages and lime calcination in a lime kiln.
    PRI me R 2 (Fig. 3). The thick liquor, similar to that used in Example 1, is first subjected to pyrolysis at 650-750 ° C in order to produce a gas containing hydrogen sulfide, carbon monoxide, angled gas, hydrogen and water vapor and a partially melted phase consisting mainly of sodium carbonate and solid carbon. The energy supply is achieved by introducing sufficient air to provide partial combustion.
    The resulting mixture of sodium carbonate and carbon is sent to a plasma reactor, in the reaction zone of which the temperature is maintained at 1200 ° C. In this case, half the amount of energy needed is required when a thick board is introduced directly into the plasma generator, as indicated in Example 1.
    In terms of one kmol, the plasma generator supplies energy of 150 kWh and introduces 2.8 kmol C and 2 kmol F j The resulting melt contains 0.1 kmol and 1.3 kmol NaOH, and in the gas it contains L tc, kmol : WITH 3.0; CO 2 0.7; Ng 1.0; 0.7.
    With the help of the gas obtained at the stage of pyrolysis, the melt can be converted into chemical substances of the liquor from the sulphate Varm and into the gas, which contains almost no sulfur. Alternatively, the melt obtained from the plasma reactor stage after dissolution can be directly used in other processes as a bleach. Therefore, this process can be considered as an alternative to the usual electrolytic method of producing sodium hydroxides; in the electrolysis method, gas chlorine is necessarily formed as a by-product.
    权利要求:
    Claims (5)
    [1]
    In comparison with the known method, the proposed method allows one to control the temperature and the oxygen potential during the processing of the liquor, to carry out the process at a lower temperature and to reduce the amount of carbonate sodium in the final product. Invention Formula
    I. A method for producing chemicals from spent liquor from sulphate pulp production, including feeding spent liquor into the reaction zone of a reactor, heating it, cooling the resulting products and withdrawing them from the reactor in the form of a melt or aqueous solution containing sodium hydroxide and sodium sulfide, and containing hydrogen and carbon monoxide, which is different from that with the aim of simplifying the process and providing the possibility of individual control of temperature and oxygen potential during the processing Lok, heating spent liquor osushestvl removed via a plasma generator and the process is conducted at a
    generator 1000-1300 s.
    five
    0
    five
    [2]
    2. The method according to p. 1, about t l and u and u so that the cooling
    Part of the received products is at 600-900 C.
    [3]
    3. A method according to claim 1, characterized in that prior to being fed into the reactor, the spent liquor is subjected to pyrolysis in air at 650-750 ° C to form a melt containing sodium carbonate and carbon, and a gas, while the melt is directed to the reactor.
    [4]
    4. A method according to claim 3V, characterized in that the gas obtained at the pyrolysis stage is treated with a melt withdrawn from the reactor to form chemical substances of the spent liquor and depleted
    gas.
    I
    [5]
    5. A method according to claim 3, characterized in that the gas obtained at the pyrolysis stage is burned to form sulfur dioxide and carbon dioxide and treated with the melt withdrawn from the reactor until the formation of sodium sulfite and sodium bisulfite.
    liZ.i
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    同族专利:
    公开号 | 公开日
    NO841299L|1984-10-22|
    FR2544758A1|1984-10-26|
    ES8501468A1|1984-12-01|
    GB2138458A|1984-10-24|
    FI841283A|1984-10-22|
    SE448007B|1987-01-12|
    SE8302245D0|1983-04-21|
    CA1222605A|1987-06-09|
    FI74499B|1987-10-30|
    FI74499C|1988-02-08|
    NZ207797A|1987-08-31|
    GB8408882D0|1984-05-16|
    US4601786A|1986-07-22|
    ID969B|1996-10-01|
    BR8401646A|1984-11-20|
    ATA121984A|1987-09-15|
    AU559424B2|1987-03-12|
    JPS59199892A|1984-11-13|
    GB2138458B|1986-12-31|
    PT78458B|1986-07-22|
    ZA842552B|1985-11-27|
    AT385531B|1988-04-11|
    FR2544758B1|1986-08-01|
    MX161274A|1990-08-17|
    JPH0424475B2|1992-04-27|
    FI841283A0|1984-03-30|
    US4692209A|1987-09-08|
    SE8302245L|1984-10-22|
    ES531644A0|1984-12-01|
    AU2649084A|1984-10-25|
    PT78458A|1984-05-01|
    引用文献:
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE8302245A|SE448007B|1983-04-21|1983-04-21|PROCEDURE AND DEVICE FOR RECOVERY OF CHEMICALS|LV920541A| LV5303A3|1983-04-21|1992-12-29|Legucanic enrichment of chemi- cals from the production of sulphate|
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