• 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:

    公开号:SU1828465A3
    申请号:SU894613905
    申请日:1989-04-14
    公开日:1993-07-15
    发明作者:Kubiak Khelmut；Yurgen Shreter Khans；Gappa Gyunter；Kalvittski Khajnrikh；Knop Klaus
    申请人:Bergwerksverband Gmbh；
    IPC主号:
    专利说明:

    The invention relates to a method for gasification of coal under pressure with water vapor in a gas generator with heat exchange tubes located inside it for a heat transfer medium, as well as gas generators with a fluidized bed for implementing this method.
    The basis of the invention is the task of improving the method of the type mentioned above for the optimal use of the introduced heat, as well as creating a re with heat exchange tubes located inside it for the heat transfer medium, while the hot heat transfer medium flowing through the heat exchange tubes into the gas generator is first introduced into the gasification zone, and then fed into the pyrolysis zone, and the coal to be gasified is led through the gas generator using the counterflow method, as a result of which coal is already used to heat the pyrolysis coolant flow, while heat for gasification bleed still hot coolant flow. Suitable for implementing the method according to the invention are vertical and horizontal gas generators of an appropriate design. Coal supply is carried out using superheated steam or circulating crude gas. An unrefined circulating gas is additionally introduced into the pyrolysis zone as an additional means of fluidization and coolant, the ash particles are cooled by the dry gas or water vapor, the temperature of which is 20,000 ° higher than the dew point. 2 sec and 5 zpp-fs, 2 ill., 2 tab.
    gas generators suitable for this task.
    The hot heat transfer medium entering the gas generator through heat exchange pipes is first introduced into the gasification zone, and then transferred to the pyrolysis zone, and the angle to be gasified is led through the gas generator using the counterflow method, due to which an already cooled heat carrier flux is used to heat the pyrolysis of coal, while how warm for gazi
    fications are taken from a still hot heat-carrying stream.
    Due to the consistent location of the gasification and pyrolysis zone relative to the coolant, all energy at high temperature - which favorably affects the kinetics, i.e. gasification rate - enters the gasification zone. Then the entire heat carrier with a lower inlet temperature passes into the pyrolysis zone and provides there the heat demand for the heating and pyrolysis process.
    The consequence of the fact that the introduction of the coolant and gasification means is carried out by the countercurrent method, is a significant improvement in the use of heat from the heat transfer medium. The reduced temperature does not have a kinetic effect on the pyrolysis reaction, since here the high temperature is less important than the presence of a sufficiently large amount of heat. The latter is provided by the large mass flow of the coolant and the corresponding dimensions of the heat exchangers.
    Water vapor, in addition to gasification and fluidization, can also serve as an additional supplier of coolant for coal gasification, in order to increase the gasification performance by increasing the temperature.
    The supply of coal is preferably carried out by means of circulating crude gas or superheated water vapor with a temperature of the order of 700-800 ° C., so that the resins resulting from the pyrolysis are cracked into gaseous hydrocarbons, preventing the condensation of the resins in subsequent apparatuses.
    It is recommended that the fluidization of coal particles is carried out with superheated water vapor, which is introduced, preferably at a temperature of 700 ~ 800 ° C, into the gasification zone, due to which the amount of heat from the heat-carrying medium is used exclusively for gasification.
    The fluidization and cooling of the ash particles can be carried out in a separate cooling zone using water vapor, the temperature of which, preferably. exceeds the dew point by 20-100 ° C, depending on pressure, in order to use the heat of ash particles at a high temperature level.
    The ash particles are cooled by water vapor in apparatuses of a vertical construction, preferably in a moving layer, in order to change the demand for water vapor. ___
    Coal loading is preferably carried out in the pyrolysis zone and is carried out using one or more jet feeders in order to avoid agglomeration of coal particles.
    It is recommended to unload chilled ash from the cooling zone through the discharge gateway. A similar discharge gateway for hot material is known.
    It is recommended to use flue gas as a heat carrier gas, preferably with a temperature of the order of 950 ° C, which, due to its high density, transfers large amounts of heat and can be obtained from the products of these processes during subsequent processes.
    As the heat carrier gas, helium can be used, which can be taken from the secondary circuit of a high-temperature reactor with a temperature of about 900 ° C or from a primary circuit with a temperature of up to 950 ° C and which has good heat transfer properties.
    The fluidized bed gas generator for implementing the method according to the invention is characterized in that. that the cylindrical pressure tank of the horizontal gas generator is subdivided into a heating and pyrolysis zone, a separate gasification zone, and also a separate cooling zone, that the heating and pyrolysis zone is equipped with openings for loading coal and introducing unrefined gas or steam into the form of a jet feeder, which the gasification zone has openings for supplying steam connected to the streamlined bottoms, that in the cooling zone there is a hole for supplying steam and a flowing bottom and an unloading lock that The heating and pyrolysis zones contain an inlet for supplying heat carrier gas and heat exchange pipes, as well as an internal or external connecting pipe connected to the heat exchange pipe and the heat carrier gas outlet in the gasification zone, which is impermeable to gas between the gasification zone and the heating and pyrolysis zone and solids partition and that above the said zones there is a gas collector chamber with a gas outlet.
    The horizontal design of the gas generator provides significant savings in water peer due to the fact that the water vapor introduced into the gasification side of its partial conversion in this zone is combined with the raw gas from the heating and pyrolysis zone and partly after the regenerative heat transfer rushes into the pyrolysis zone, as a result of which the gas generator does not occur additional need for water vapor. !
    The water vapor content in the gasification zone can be maintained at a very high level, which in turn has a positive effect on their kinetics. Unconverted water vapor is completely 1 sufficient to cover the need for secondary pyrolysis reactions in the heating and pyrolysis zone after partial recirculation in the form of moist crude gas. 1
    The horizontal design of the gas generator with a barrier impenetrable for solids has the advantage that it is possible not only to subdivide into two stages, but also additional cascading in the gasification zone. This further prevents the so-called back-mixing.
    In a horizontal fluidized bed gas generator, it is advisable to provide in the heating and pyrolysis zone an additional supply of circulating crude gas and a streamlined bottom and to integrate heat exchangers and a gas pump in the gas return line.
    Another design of a fluidized bed gas generator for implementing the method according to the invention is characterized in that the cylindrical pressure tank of the vertically mounted gas generator is divided into a heating and pyrolysis zone located in the upper part and a separate gasification zone located below it, as well as a separate cooling zone located below the heating and pyrolysis zone is provided with openings made in the form of a jet feeder for loading coal and supplying crude circulation gas, or ara, that the gasification zone is equipped with a steam supply opening connected to the streamlined bottom, that the cooling zone is equipped with a steam supply opening connected to the streamlined bottom, and an unloading lock, that in the heating and pyrolysis zone are located the gas-coolant inlet and heat exchange pipes and the connecting a pipeline, the latter being connected to a heat exchange pipe, and the removal of heat carrier gas in the gasification zone, which between the gasification zone and the heating and pyrolysis zone is provided for permeability to gas and solids odka and that over heating and pyrolysis zone is the gas plenum with venting.
    The advantage of gas generators of a vertical design is that a significant amount of water vapor is saved, since water vapor introduced into the gasification zone after its partial conversion in this zone, together with the produced gas, flows O directly into the pyrolysis zone, as a result of which there is practically no additional need for water pair in this zone.
    At the same time, another 5 advantage arises, namely, that in the gasification zone the water vapor content can be maintained at a high level, which positively affects the kinetics. Water vapor that has not undergone O conversion in the gasification zone is sufficient to cover the need for a peer to convert the resin in the pyrolysis zone.
    Another advantage of the vertical gas generator 5 is that the location of the pyrolysis and gasification zones * above each other makes it possible to separate both zones by a partition permeable to gas and solids. The division into two stages achieved by this (cascading) significantly reduces the undesirable mixing of newly introduced fuel with fuel from the gasification zone (the so-called reverse mixing), which makes it possible to gasify with a high degree of conversion.
    Further advantages in comparison with other methods are inherent in gas generators of both vertical and horizontal design due to the cooling of residual coke in the cooling zone.
    In horizontal gas generators, the residual coke after it is transferred from the gasification zone to the cooling zone is cooled with produced gas or low-temperature steam, the temperature of which is 20-100 ° C higher than the dew point so as to prevent reaction inhibition in the gasification zone • adjacent . Due to this, firstly, it is achieved that the residual coke is cooled to a temperature at which more than 5 technically simple discharge is provided. Secondly, an even greater benefit is achieved from the fact that - especially with partial gasification - the heat of the resulting coke breeze is used more efficiently.
    Ί 1 828 465 8
    In Fig.1 a gas generator of vertical construction / construction; figure 2 - gas generator of horizontal design.
    Figure 1 shows the pressure tank 1, divided into four zones, 5 located in the gas generator 19 of a vertical design one above the other. The upper zone is a gas collector 15, from which gas can be discharged through the pipe 21. To the next zone, heating zone 2 and pyrolysis through the connecting pipe 6, fine coal dust as gasified material at a temperature below the softening point and steam as a means of gasification with a temperature of the order of 700 - 15 800 ° C pneumatically dosed using a jet feeder 5. In the cylindrical part of zone 2 there is a connecting pipe 9 for the removal of heat carrier gas connected to heat transfer pipes 20
    10. The diameter of pyrolysis zone 2 is brought into correspondence with the gas velocity, which is measured by the amount of outgoing gas from the gasification zone located below and the amount of gas coming from the jet 25 feeder. The heat-carrying medium is conducted by the counterflow method relative to gasified fuel from the gasification zone 3 at a lower temperature level to the pyrolysis zone 2. thirty
    Gasification zone 3 is located in the central part of the pressure tank 1. It is equipped at the bottom with a connecting pipe 7 for supplying superheated water vapor and at the top with a connecting pipe 35 with a pipe 13 for supplying a hot heat transfer medium. The latter enters at high temperature (about 900 ° С950 ° С) into heat-exchange pipes and transfers its tangible heat to gasified fuel 40 to turn it into gas. Through the connecting heat conduit 11, the cooled heat carrier gas enters the heat exchange tubes 10 in the heating and pyrolysis zone 2 and through the pipe 9 again leaves the pressure tank 45 with a temperature of about 750800 ° C. Superheated water vapor with a temperature of the order of 700-800 ° C enters the fluidized bed in zone 3 through the flow around the bottom 8. According to the design variant not shown 50 here, the connecting pipes 9 and 13 for the outlets for introducing the coolant gas can also be located next to each other in the area of the common outlet pipe. 55. The gasification and pyrolysis zone 3 or 2, in order to optimize the length of stay of the gasification means in the reaction zone (in order to reduce back mixing), is separated from each other by a partition 14 permeable to gas and solids. The partition 14 is designed so that in its extreme adjacent to the wall of the zone, preferably coal dust flows from the pyrolysis zone 2 to the gasification zone 3, which counteracts the movement of solid particles forming in the fluidized bed.
    The gasification zone 3 is adjacent to the cooling zone 4, which is still in the cylindrical part of the pressure tank 1, for the remaining fuel. The cooling zone 4 is fed through a connecting pipe 16 and a streamlined bottom 17 with water vapor, the temperature of which exceeds the dew point by 20-100 °. The cooling zone 4 preferably functions as a moving bed, but the precipitate can also be fluidized by increasing the amount of flowing steam. Under the streamline bottom 17, the pressure tank 1 tapers conically up to the connecting pipe 18, which serves to remove the cooled sediment.
    The horizontal gas generator contains a pressure tank 1, which is divided by partitions into zones 2.3.4, which are arranged sequentially one after another. In the front zone, heating and pyrolysis zone 2, through the connecting pipe 6, fine coal dust is pneumatically dosed using jet feeders 5. Through the pipe 6, wet circulating crude gas or superheated steam is also introduced, which is regeneratively or not shown here in the combustion chamber brought to high temperature level. This gas serves to fluidize and convert the originally formed coal pyrolysis products. In the upper zone of the pressure tank 1 there is a connecting pipe 9 for the removal of the heat-carrying medium, connected to heat transfer pipes 10.
    In the middle part of the pressure tank 1 there is a gasification zone 3. This area below is equipped with connecting pipes 7 for supplying superheated water vapor. Superheated water vapor is introduced into the fluidized bed in the gasification zone 3 through the streamlined bottom 8. In the shown example, heat transfer pipes 13 in the gasification zone 3 are parallel to the heat transfer medium, so that the heat transfer medium has a high temperature throughout the zone,
    The heat carrier medium of high temperature enters through the connecting pipe 13 into the gasification zone 3, there passes heat exchange pipes 12 and then through the connecting pipes 27 and the connecting pipe 11, which is located outside the pressure tank 1 in the shown example, is transferred from the gasification zone 3 through the connecting pipe 28 to lower temperature level in zone 2 of pyrolysis.
    The gasification and pyrolysis zone 3 or 2 in order to optimize the length of stay of the gasification means in the reaction zone (in order to reduce back mixing ”) is separated in this case by a partition 14, which is impermeable to gas and solid particles, between the zones 2 and 3.
    The gasification zone 3 is also separated from the adjacent cooling zone 4 by a partition 14 impermeable to gas and particulate matter. The cooling zone 4, in order to cool the residual coke or, if necessary, for fluidization, is supplied with steam having a temperature close to the temperature of saturated steam, or, preferably, dry exhaust gas through the connecting pipe 16 and the flow around the bottom 17.
    On top of the cooling zone 4 is a connecting pipe 21 for venting gas. This nozzle is connected to the upper part of the housing by a gas collector 15, extending in the longitudinal direction above the successive zones 2,3,4.
    Through the connecting pipe 22 wet wet basin can be introduced. through the flowing bottom 23 to the heating and pyrolysis zone 2. In this example, this circulating gas is preheated in heat exchangers 24.25 and is directed to the connecting pipe 22 using a gas pump 26.
    The ash sludge is unloaded from the cooling zone 4 through a connecting pipe 18, preferably through a lock not shown here.
    A comparison is made of the essential indicators of the new method for allothermic gasification of coal with the previously known method of coal gasification by water vapor. For better comparability, the thermal power of the heat source is 340 MW. When carrying out full gasification (Table 1), the method according to the prior art using a gas generator of horizontal construction contrasts the methods using a gas generator of horizontal and vertical construction according to the invention. When implementing partial gasification (Table 2), for the implementation of which a vertical structure gas generator is particularly effective, comparison is made only between the method according to the technical level and the new method according to the invention using a vertical structure gas generator.
    From the table. 1 shows that when implementing the method according to the invention with the same thermal power of a heat source equal to 340 MW, and with the same degree of conversion of coal equal to 95%, a vertical gas generator with a slightly increased productivity for 15 coal processing has a significantly lower consumption of water vapor than in the implementation of the method according to the prior art. This is mainly the result of features of the invention and pressure reduction. When using a horizontal gas generator, • along with the same benefits of reduced water vapor consumption. the benefits are shown in a 25-fold almost double increase in coal processing capacity, as well as a significant improvement in the use of high-temperature heat.
    Similar advantages are also observed30 in the case when only partial gasification should be carried out for the simultaneous production of coke breeze (Table 2). Compared to gasification, which provides 95% conversion, a vertical gas generator35 at 50% conversion has the advantage of significantly greater coal processing capacity compared to the method used in accordance with the current 40 prior art.
    权利要求:
    Claims (6)
    [1]
    Claim
    1. The method of gasification of coal under pressure with water vapor in a gas generator with heat pipes 45 inside, for a coolant, which consists in. that coal is supplied to the gas generator, it is fluidized with water vapor in the fluidized bed, the coal is heated in the heating and pyrolysis zone and the gasification zone with alothermic heat transfer fluid passing through the heat exchange tubes, the heat transfer being first fed to the gasification zone, then to the heating and pyrolysis zone, and coal the gas generator passes in countercurrent to the coolant, characterized in that, in order to optimally use the introduced extraneous heat, the coal is supplied using superheated steam or circulation neo of purified gas, circulating crude gas is additionally introduced into the pyrolysis zone as an additional means of fluidization and coolant, the ash particles are cooled by the dry gas or water vapor, the temperature of which is 20-5100 ° higher than the dew point.
    [2]
    2. The method according to claim 1, characterized in that the coal is charged by one or more jet feeders. 10
    [3]
    3. The method of pop 1 or 2. characterized in that the discharge of chilled ash from the cooling zone is carried out through the discharge gateway.
    [4]
    4. The method according to claim 1, 2 or 3. - I distinguish between 15 and тем with the fact that flue gas with a temperature of about 950 ° C is used as the heat carrier gas.
    [5]
    5. The method according to claims 1 and 2, characterized in that helium from a secondary circuit, a high-temperature reactor having a temperature of about 900 ° C, or from a primary circuit having a temperature of up to 950 ° C is used as a heat carrier gas. .
    [6]
    6. Gas generator with a fluidized bed, containing a cylindrical horizontally located pressure tank, partitions located in the tank in the region of the fluidized bed, impermeable to gas and solid particles and dividing the tank into three zones: heating and pyrolysis zone, gasification zone and the third zone, gas distribution means located in zones, a pipe for supplying coal connected to a zone of heating and pyrolysis, pipes for supplying steam connected to a zone of gasification and gas distribution . heat exchange pipes located in the tank in the heating and pyrolysis zone and in the gasification zone and having a heat-carrier gas inlet in the gasification zone, a gas outlet connected to the upper part of the tank. from the fact that, in order to optimally use the introduced extraneous heat, it additionally contains jet feeders connected to the reservoir in the heating and pyrolysis zone with nozzles for supplying coal and circulating raw gas or steam, a nozzle for introducing steam or produced gas, connected to the third zone of the tank, designed for cooling ash, an additional heat exchange pipe located in the gasification zone, a connecting pipe located inside or outside the tank, connected single to the exits of the heat exchange pipes of the gasification zone and the inlet of the heat exchange 25 pipes of the heating and pyrolysis zone, the upper ends of the partitions being installed with a gap relative to the upper part of the tank to form a common gas collector connected to the gas outlet.
    30 7. The gas generator according to claim 6, characterized in that it comprises a circulating raw gas supply system including heat exchangers and a gas pump connected to the gas outlet and gas distribution means of the heating and pyrolysis zone.
    Comparison with full gasification (95% conversion)
    Indicator The method according to the invention The method according to the prior art (gas generator-horizon, design Horizontal gas generator D gas generator of a vertical design Thermal power of a heat source, MW 4x85 = 340 2x170 = 340 1x340 The number of gas generators 4 2 1 Dimensions of gas generators length / height, m 18 20 33 outer diameter m  5,0 7.0 7.0 Pressure bar 21 21 44 The degree of conversion of coal,% 95 95 95 keuglya, t / h Specific consumption of water vapor 60.0 30.5 27.3 t NgO 2.67 2,53 6.95 hmda —-------- i ----
    Continuation of the table. 1
    Indicator The method according to the invention The method of technology level (gas generator horizon, design Horizontal gas generator D gas generator of a vertical design The degree of decomposition achieved by water vapor,% 49 52 19 The use of high temperature heat,% 21.6 10.0 9.4 *
    table 2
    Partial gasification comparison (50% conversion)
    Indicator The method according to the invention The method according to the prior art Vertical gas generator Horizontal gas generator Thermal power of a heat source. MW 2x170 = 340 1x340 The number of gas generators 2 1 Dimensions of gas generatorslength / height, m 20 33 outer diameter m 7.0 7.0 Pressure bar 21 44 The degree of conversion of coal,% fifty • fifty Coal processing capacity, t / h 112.0 84.6 „. t Н 2 О Specific consumption of water vapor ----- t coal 0.99 2.44 The degree of decomposition achieved by watersteam,% 52 21.1 The use of high temperature heatla,% 19.6 13.7
    Fie 1 fig 2
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3635215A|DE3635215C2|1986-10-16|1986-10-16|
    PCT/EP1987/000605|WO1988002769A1|1986-10-16|1987-10-15|Process and fluidized bed gas generator for allothermic gasification of coal|
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