• 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:
    Pulverulent fuel e.g. dried lignite is supplied to a suspension gasifier under pressure from a lock hopper (5) into a dosage container (7), the powder heap is partially fluidized by a carrier gas and the carrier gas, charged with pulverulent fuel, is passed by a feed line (9), towards the burner(s) (30) of the gasification reactor (31), the ratio of internal cross-sectional area of the feed line to the free cross-sectional area of the partially fluidised layer is arranged to be from 1:50 to 1:300 and the power stream is regulated by varying the carrier gas stream, injected into the lower part of the dosage container (7) in accordance with the powder flow or a parameter measured in the gasifier. <IMAGE>
    公开号:SU1167194A1
    申请号:SU787770281
    申请日:1978-08-21
    公开日:1985-07-15
    发明作者:Бархманн Лутц；Гелер Петер；Кретшмер Хорст；Шигнитц Манфред；Швейгел Ханс-Йоахим；Титце Гюнтер
    申请人:Бреннштоффинститут Фрейберг (Инопредприятие)；
    IPC主号:
    专利说明:

    The flow of dust to the amount of oxygen flowing per unit of time to the burner.
    2. Method POP1, characterized in that an alternate operation of several, preferably two, sluice high pressure vessels before the dosing unit is performed in such a way that, constantly or, excluding short switching periods, up to a maximum of 10% of the total time, at least one sluice container high pressure to ensure unloading is connected to the dispenser.
    3. Method according to paragraphs. 1 and 2, that the unloading of the lock vessel or high pressure vessels into the dispenser is carried out through a coarse dose device or through an adjustable throttle device for flow, and for example, a coarse dose device or an adjustable throttle device is used. compression closed cell drum, dosing screw for coarse dosing or gate and using a known method of measuring the filling level
    in the dispenser, by impulse control of the coarse dispensing device or the throttle device, it is produced so that within certain limits the level in the dispenser remains constant.
    4. Method according to paragraphs. 1-3, which is due to the fact that in order to set the pressure in the lock vessel
    or high-pressure vessels and technical nitrogen or a mixture of nitrogen and air with an oxygen content of less than 6%, technical carbon dioxide, foreign-made combustible gas, own-produced return gas produced by this method, or a mixture thereof are used as carrier gas.
    5. Method according to paragraphs. 1-3, characterized in that the pressure in the lock vessel or high pressure vessels is adjusted by an inert gas, such as nitrogen, with a maximum oxygen content of 6% and / or carbonic acid gas, a combustible gas is used as the carrier gas.
    6719A
    6. Method according to paragraphs. 1-3, which is based on the fact that the pressure in the lock vessel or high pressure vessels is adjusted by inert gas, such as nitrogen, with a maximum oxygen content of 6% and / or technical carbon dioxide, air is used as the carrier gas. or a mixture of oxygen with an inert gas with a maximum oxygen content of up to 21%.
    7. Method according to paragraphs. 1-6, which is due to the fact that dried, ground to grain size, preferably less than
    . 0.5 mm and with a moisture content of up to 12% storm coal, the velocity of the carrier gas in the free section at the bottom of the dispenser is 0.0050.025 m / s, and the speed of the mixture is the dust of the carrier gas in the conveying pipeline from the bottom dispenser to the burner 1.0-7.0 m / s.
    8. Device for gasification of pi-type fuels under. The length of the dispenser is that the dispenser consists of a shaft-like upper part, preferably a circle, a logo of the section and of the lower part, open with respect to the shaft-shaped upper part, or several lower parts, open with respect to the upper shaft-shaped part or from one open with respect to the upper shaft-shaped part and into several sections of a divided lower part, with the lower part or each of the lower parts, or each part of the lower part having a flow bottom that has at least one connection for the flow oreguliruemogo input audio gaseous medium, wherein in its or their inner space
    , through the side wall or through the flow bottom or the shaft-like upper part of the dispenser, one or several employees serving as a conveyor pipeline: a house of pipes that are connected to the burner or burners of the gasification reactor.
    9. The device according to claim 8, characterized in that the lower part of the dispenser has a smaller section than the shaft-like upper part, fitting the section of the upper part
    to the cross section of the lower part or parts, or to the section of separated sections of the lower part, is carried out in such a way that the loose pulverized fuel mass in the upper part of the dosing unit slides down the section evenly and without forming funnels into the lower part or part or divided areas of the lower part of the dispenser. 10. Device on PP. 8 and 9, characterized in that the flow plate, at the temperature conditions and pressure rates from 0.005 to 0.025 m / s provided for the carrier gas, has a related pressure loss over the entire cross section of the bottom that is equal or greater than the value of the product weight and height of the bulk powder mass in the dispenser. 11. Device on PP. 8-10, characterized in that in the supply line of pulverized fuels to the metering unit, a known coarse metering device or an adjustable throttle device and a feed over it are installed for the flow of drums. a coarse dose device or over an adjustable throttle device is branched so that two or more high-pressure sluice vessels can alternately be discharged into the doser; the upper part of the dispenser is equipped with a known device for measuring the level, which is connected with the coarse dosage device or by means of a throttle device, the magnitude and time of the cycles for decreasing the pressure of filling, pressure build-up and discharge of the high-pressure sluice vessels are consistent with each other so that Exclude short periods switching maximal 10% of the time for Men necks least one sluice vessel 94 of high pressure through a rough dosing device or adjustable throttle device is connected to the dispenser to allow unloading. 12. The device according to claim 11, wherein the sluice high pressure vessels have corresponding known filling level gauges that affect the adjustment of the valves of the sluice high pressure vessels, so that when reading the minimum filling level and zero level in one A pressure vessel connected to unloading with a metering device is switched over to another pressure vessel-filled pressure vessel filled with pulverized fuel. 13. The device according to paragraphs. 8-12, differing from the fact that in the transporting piping or pipelines going from the bottom or bottom parts, or from the separated sections of the bottom part of the dispenser to the burner or the gasification reactor pressure switches, are known measuring devices flowed to the burner, which through the regulator affect installation fittings or fittings in the supply or supplies of gas-carrier to pro-. exact bottoms or flow bottoms. 14. The device according to paragraphs. 8-12, differing in the fact that the measuring instrument establishes in the gasification reactor a value depending on the dust flow or on the ratio of the dust flow to the incoming burner to the burner per unit amount of oxygen, preferably the temperature in the reaction space of the reactor, acts through the regulator fittings or fittings in the supply or supply lines for carrier gas to the flow plate or flow plates.
    one
    The invention relates to methods and devices for gasification under
    pressure of pulverized fuels for the production of gases containing CO and H, 3 which, directly or after further purification, can be used as combustible gas, synthesis gas, reducing gas, a mixing component for city gas, etc. Shredded are used as pulverized fuels to fine dust, lignite and hard coal, as well as finely divided solid carbon containing coal and oil processing residues and solid carbon-containing organic materials of other origin, respectively crushed, (for example Sawdust old pokrshki, plastics waste). The possibility of gasifying pulverized fuels with an oxidizing agent containing free oxygen in the form of a fiery reaction will make the fuel more diversified. Of particular importance is the provision of reliable supply of pi-like fuel and the system under pressure and its uniform dosages of the book. In order to obtain pulp-like fuel, it is necessary to mix it with a liquid and, with the help of pumps, deliver a liquid-liquid hydrocarbon, such as fuel oil or tar, which is gasified together with pulverized fuel to the system under pressure. , T ensuring the pumpability and the maximum solid / liquid ratio (depending on the structure and calorific value of pulverized solid fuel), as a rule, only 30–40% of the total energy supplied to the fuel can be covered with dust with solid fuel, while used to obtain a pulp liquid hydrocarbon. Whether pulp production can be applied and water in this case, using appropriate pumps, the dust – water mixture brought to the pressure of the gasification system passes through a booster in which the water evaporates and overheats so that the dust – steam mixture is supplied to the gasification reactor itself. Especially with porous, hygroscopic fuels, such as soft brown coal, for its reliable pumping capacity, the proportion of water is so high that after evaporation and overheating 44 water vapor-dust ratio exceeds the optimum value necessary for the gasification process. Therefore, it is necessary to separate part of the water vapor or water from the suspension inside the system under pressure or to use the additional costs of oxygen in the gasification process in order to ensure that the temperature in the reactor is sufficient for processing dust in spite of the high excess of water vapor. Such drawbacks are characteristic when mixing one part of dust with water and another part of dust with liquid hydrocarbon, as described in DE-OS 2536 249. Methods are known for gasifying dust-like fuels under pressure, according to which dust is fed through a periodically operating lock vessel of high pressure. an intermediate vessel that is pressurized with gasification. From this vessel, a fluid intake by means of a mechanical metering device, for example, an auger with an adjustable rotational speed, is fed into a stream of carrier gas, which transports pulverized fuel to the burner of the reactor. Oxygen, water vapor and / or COj, nitrogen, combustible gases of other origin, or return cooled and purified gas obtained in the process itself are used as the carrier gas. To ensure a satisfactory supply of pulverized fuel to the burner, relatively high speeds are required in the conveying pipeline from the mechanical dosing device to the burner and at high gasification pressure a large amount of gaseous carrier media. This leads to increased specific oxygen consumption depending on the type of gas used for transportation. and the level of inert gases (N) in the resulting gas, laborious associated with the loss of recompression and the reverse flow of large amounts of of gas. In the case of application in a burner of technical oxygen as a carrier gas with a normal pressure, the danger of formation of explosive dust-oxygen mixtures in the approach to the burner and in the burner, as well as the danger of a reverse blow of the flame with increasing technological pressure, increase. Therefore, this option is unacceptable in gasification processes under pressure. This group of methods is also characterized by unsatisfactory operation of the mechanical dosing device in the system under pressure, since the high dosing accuracy depends on sensitivity to interference or frequent repairs. The same problems are characteristic of the group of methods, according to which the dust supply to the system under pressure occurs through a continuously or quasi-continuous dust pump according to the principle of centrifugal force (DE patent 2617490) or displacement principle (DE patents 1252839 and DE 1262494). To supply and meter coal dust to a gasification reactor, a fluidized bed system is used, consisting of a high-pressure lock vessel, in which the pulverized fuel in an alternating process, by introducing inert gas, is brought to the pressure of the gasification system and a pressure vessel, in which the fused fuel is bypassed. a sluice pressure vessel and in which an inert gas is blown up, fluidization of the fuel occurs. From this vessel a stream of dust along with a part of an inert gas, which is used for fluidization, is a post. It goes to the burner of the gasification reactor; The magnitude of the flow is determined by the density of the fluidized bed and the difference in pressure between the pressure vessel and the gasification reactor. In such a device, the system (Ulman’s Industrial Gas Encyclopaedia, Vol.10. - Gasification of coal) achieves a very large ratio of solid substance to gas (about 3QO kg / m of carrier gas). However, maintaining the fluidized bed requires a circulation line of a fluidizing inert gas with laborious dedusting installations and compression, so that the known solution is also unacceptable. (Meunier. Gazi4 ficatsi and oxidative transformation of fuels, Weingheim, 1962). The purpose of the invention is to create a method and device for gasifying dust-like fuels under higher pressure with high uniformity and reliability and low flow rate of carrier gas in the system for supplying, metering and supplying dust to the gasification reactor burner. The task of the invention is to create a method for gasifying pulverized fuels under higher pressure, preferably at pressures of 550 bar, at which the feed is dusty. Tomniaa visible in the system under pressure, its dosage and supply to the burner of the gasification reactor occurs with the help of carrier gas. According to the proposed method, high feed ratios of solids to gas carriers (in the operating state of 300 kg / m of carrier gas) and high specific feed rates in the feed to the burner and, in addition, high accuracy of the flow of dust to the burner, reduced gas consumption are achieved. carrier to maintain fluid beds and high operational reliability. The method is carried out in the following manner. The pulverized fuel used for gasification from a spare bunker under atmospheric pressure is fed to a lock vessel of high pressure. Injecting compressed inert gas. HanpiiMep nitrogen or carbon dioxide, the pressure in this lock vessel is adjusted to a pressure that slightly exceeds the pressure in the gasification reactor. The pressurized pulverized fuel is fed to the next pressure vessel, the dispenser. At the bottom of the metering device. By supplying a gaseous medium, the dry mass of dust is loosened so that the pulverized fuel, along with the carrier gas, is supplied through a transporting pipeline, starting at the bottom of the metering unit and projecting into the bottom of the metering unit, to the gasification burner. The ratio of the free section of the conveying pipeline to
    7
    the free section of the lower part of the dispenser is (1:50) - (1: 300).
    The fuel in the lower part of the dispenser is loosened to the crumbly (limited to the lower part) fluidized bed.
    The bulk mass of pulverized fuels lying above the bottom of the metering device has the character of a calm mass, which, in accordance with the selection of the pulverized fuel to the gasification reactor, slowly slides down and is usually washed only by gas (relatively small), the amount of which corresponds to the volume of solids in the selected dust dispenser.
    The carrier gas stream is saturated with a fluid fuel, for example 500 kg of dust per 1. m of carrier gas in the process with a net dust density of 1.4 g / cm. By changing the amount of carrier gas at the bottom of the metering unit, the flow of dust entering the reactor (kg of galliform fuel per unit of time) can be controlled, and in a wide range the saturation ratio of dust to carrier gas remains constant. Therefore, the adjustment of the fuel supply to the gasification reactor is carried out by a corresponding change in the carrier gas flow to the bottom of the metering device.
    As an impulse regulator, for example, direct measurement of the dust flow in the supply line to the burner, differential measurement of the filling of the dispenser, or a value that depends on the supply of dust or the ratio of dust oxygen can be used, for example, the temperature set in the reaction space of the reactor can be used.
    The dust that serves to divert the flow — a carrier gas protruding into the lower part of the conveyor dosing unit can be brought into the loosened part of the bulk mass horizontally or vertically from below or from above. The continuity of transport due to changes in the direction of supply of the transporting pipeline to the burner does not have a negative effect with sufficiently large radii of the knees. AT
    1671948
    This may result in any arrangement of the dispenser and the reactor. In addition, at certain points in the pipeline, it is possible to additionally bring up very small amounts of carrier gas, in order to ensure that transportation is not perfect.
    Dosing accuracy of pulverized fuel, i.e. reverse value
    The range of fluctuations of the instantaneous values of the fluidity of dust reduced to the average dust flow is the higher, the less the level of loose mass is subject to fluctuations in the dispenser.
    . If the dispenser is packaged with
    pressure vessel, it should be relatively large, in particular, have a relatively large cross-section in the upper
    parts so that the relative fluctuations in the level of the bulk mass in the dispenser can be maintained sufficiently low during the filling and pressure cycles
    and reducing the pressure in the pressure vessel. Therefore, in another embodiment, the proposed device provides for the arrangement of two or more parallel-working high-pressure sluice vessels, which are filled and discharged alternately in the dispenser. As a result of gravity, the high-pressure dispensing sluice vessel is discharged through an adjustable throttle body installed above the dispenser for flow of slurries controlled by measuring the level of loose mass in the metering device.
    Known measuring instruments for measuring the filling level in sluice high pressure vessels, after unloading the first airlock, ensure the flow of dust from the second
    pressure reduction, new filling and pressure set of the first oshyuz and vice versa.
    Since the accuracy of adjusting the flow of dust to the dispenser is less in order of magnitude than with the dosage of the flow of dust to the burner, in an adjustable throttle body
    Pots are low-wearing and maintenance-free devices, such as cell drums or gate valves.
    911671
    The proposed device is most effective if the number and size of sluice high pressure vessels and also the time of filling cycles to reduce pressure, set pressure 5 and unload the vessel and the rhythm of switching on individual vessels are coordinated with each other so that at each moment of time at least one vessel is associated with a dispenser for unloading or there is only a short pause of switching (up to about 10% of the total time) between disconnecting the emptied vessel and connecting the filled and being-15 seconds under the pressure of the vessel.
    A pressure vessel may be equipped with known devices for measuring the filling level, which signal the minimum or zero level of the vessel and at the same time switch to a filled pressure vessel of another vessel.
    The lower part of the dispenser, where the partial fluidized bed is maintained, is made of a smaller diameter than the upper one. Therefore, a narrowing of the upper part to the diameter of the lower part is provided, for example, with the help of turned-on intermediate parts, and this narrowing, depending on the fluid capacity of the pi-tops, should ensure a uniform decrease in the level of loose mass j without forming funnels.
    In order to ensure a very high ratio of density of the pulverized fuel to the carrier gas (more than 400 kg / m in working condition) and 40 high streams of dust, the diameter of the feed line to the burner should be maintained optimal. The ratio of the cross section of the transport pipeline to the cross section of the lower part of the dispenser depends on the installation capacity and the flow properties of the dust and is in the range (1:50) (1: 300). 50
    The uniformity of the dust suspension is the carrier gas supplied to the burner, and the accuracy of controlling the flow of dust is achieved if, through the entire cross section, 55 there is a significant homogeneous distribution of the carrier gas supplied to the bottom of the dispenser. therefore
    9L10
    the carrier gas is supplied to the loose dust mass through the flow plates of porous material, which, during normal operation, have a pressure loss that corresponds to the weight of the pulp mass per unit cross-sectional area. As a material for flow plates, for example, metal-ceramic plates, felt plates, etc. can be used.
    In order to achieve optimum performance of high reliability against the danger of oxygen breakthroughs in the cold parts of the installation connected after the reactor, in case of burner damage and damage, the gasification reactor is equipped with two OR several independently working burners. In this case, according to the number of burners, several dosing units with They are equipped with pressure vessels and other devices.
    The dispenser may have several lower parts or a lower part divided into several separate sections. In each of these lower parts or in each separate section of the lower part, a partial fluidized bed and dust can be reproduced through the immersion into the corresponding lower part. the pipeline or its section is supplied to one of the separate burners. At the same time, the fuel from the common upper part of the dispenser slips into separate lower parts or into separate parts of the lower part.
    To set the pressure in one or several sluice vessels of high pressure, the same gaseous medium can be used as a carrier gas, for example nitrogen, carbon dioxide, self-produced combustible gas, reflow gases, gases of other origin or mixtures of these gases. . In order to avoid the formation of flammable and explosion-hazardous mixtures of coal fuel, inert gas and oxygen in a sluice pressure vessel, depending on the type of preparation of pulverized fuel, it is necessary to limit the oxygen content to values below 6%. Water vapor can also be used, however, in this case, high superheating of this steam and / or high heating of the pied fuel is necessary to prevent condensation of water vapor on pulverized fuel, as a result of which steam is irrational. Air or a mixture of inert gas with oxygen with oxygen content up to 21% can be used as a carrier gas to set the pressure in the sluice vessel (s) of high pressure, since the concentration of mixtures of gas and air — carrier gas in each phase of the production process lies vppe limit explosion. In this case, the oxygen contained in the carrier gas is used in the gasification process, thus reducing the oxygen demand for gasification and at the same time reducing the level of inert gas in the raw gas by about 20%. A possible application is for pressure in an inert gas lock in a sluice vessel, preferably nitrogen and as a carrier gas of own or other production gas. In this case, the combustible gas flows fully into the gasification reactor so that the calorific value contained in this gas is used in the process. At the same time, this gas is a cheap inert gas, which, after dedusting, can be released into the atmosphere without significant pollution and environmental hazards. Figure 1 shows the scheme for the implementation of the method of gasification under pressure of pulverized fuels i in Figure 2. diagram of the supply and dosage system of the pi-shaped fuel, an embodiment with one lock pressure vessel; fig. 3 shows the same version with alternating operation of two sluice high pressure vessels; Fig. 4 is a diagram of a dozer with one lower part divided into three sections for supplying three separate burners of a gasification reactor; Fig. 5 shows a supply and dosage system for pulverized fuel according to a variant with a doser according to 9D12 but Fig. 4 and three separately adjustable burners. . I. According to an embodiment of the method according to FIGS. 1 and 2, coal dust with a particle size distribution of about .10% of the residue on a 0.2 mm sieve and a moisture content of approximately 10% is pneumatically supplied through pipe 1 of coal dust to the spare bin 2. After separation of the coal dust transporting gas through the filter 3 leaves the system. In this case, the supply of coal dust to the reserve bunker 2 is controlled by the device 19 for measuring the level. After a decrease in pressure in the lock pressure vessel 5 and the opening of the closure body 4, the brown coal from the spare hopper 2 enters the lock pressure pressure vessel 5. At the same time, the filling level of the high pressure lock vessel is controlled by a level gauge 18, which gives signals at the maximum and minimum levels. When the maximum level is reached, the closure body 4 and the lock high pressure vessel 5 are closed through the inlet 28 and the control valve 14 is adjusted with an inert gas to a pressure i equal to the pressure of the dispenser 7 (for example 30 bar). By means of the level gauge 17, the level of brown coal dust in the metering unit 7 is controlled. If the level reaches a minimum, then the locking organ 6 under the lock vessel 5 of the high pressure is opened, so that the contents of the lock pressure vessel 5 of the high pressure are fed to the metering device at least the signal of the level gauge 18 closes the shut-off organ 6. In the empty but still under pressure sluice pressure vessel through the regulating valve 15 and the gas line of reduced pressure 29, the pressure decreases to atm as a result, the ALL BLUE high pressure vessel is ready for a new filling cycle. The dispenser 7 consists of a shaft-like upper part with a cylindrical cross-section, equipped with a level gauge 17 and from the lower part 8 with a smaller diameter, which is connected to the upper part with a conical intermediate piece.
    13
    The bottom of the lower part 8 is double, and the inner part of it is decorated in the form of a porous flow bottom. Through the control valve 10, a stream of carrier gas is introduced into the intermediate space between the outer part of the bottom and the inner part formed as a flow bottom.
    In the device according to the variant shown in Fig. 2, the same inert gas carrier is supplied through pipe 28 as it was used to set the pressure in the lock vessel. Fig. 1 shows the case where different gases are fed through pipelines 34 and 35 into the lock pressure vessel and the lower part of the dispenser. Pipeline 34 in this example supplies technical nitrogen, which is produced in the production of oxygen needed for gasification, and pipeline 35 and the circulation compressor 37 supply its own production gas.
    The gaseous medium used as the gas carrier passes through the flow bottom into the lower part of the dispenser and discharges the brown-coal pie in the lower part of the dispenser so that a local limited (partial) fluidized bed occurs. The loosened brown coal dust in a very dense phase is carried away by the carrier gas through the transport tube 9 immersed in the fluidized bed from above and the coal dust and carrier gas is thereby supplied to the burner 30 of the gasification reactor 31.
    The mass flow of the brown coal ditch in the conveyor pipe 9 in a wide range is almost proportional to the amount of flowing carrier gas. The regulation of the flow of the lignite flute to the burner is made by regulating the flow of the carrier gas by means of the control valve 10, which receives its impulse (for example, figure 2), from the device 16 for measuring the flow of dust on the pipeline 9.
    The control valve 10 installed in the reaction zone of the reactor 31 and measured at measuring point 13, which is usually a function of the flow of brown coal dust to the burner (Fig. 1), can be used as a control pulse.
    6719414
    If necessary, it is possible through the valve 11 and one or several parallel supply points 12 to introduce into the pipeline 9 small amounts of additional carrier gas. This especially during the launch period and in case of poor fluid properties of brown coal dust (for example, due to a large proportion of fibrous dreamer parts), stabilizes the flow of dust with a carrier gas and reduces the possibility of plugging the pipeline in places of turns. Brown coal dust flow through
    5, pipe 9 enters the burner 30 of the reactor 31. In the burner, the brown coal pit is in contact with a mixture of technical oxygen and water vapor, which is supplied through a pipe
    0 water 36 to the burner.
    Brown coal dust and a mixture of technical oxygen and water vapor react with each other in the reaction space of the reactor 31 in the form of a flame at temperatures of about 1500 C and a pressure slightly lower than in dispenser 7 (about 29.5 bar). The resulting crude gae passes through subsequent cooling, condensation and gas-washing installations 32 and is fed (branch 33) for further use. In the lower part 8 of the dispenser 7, 65 m in the normal state of the 5 research institutes of the carrier gas are supplied, respectively, about 2.35 m in the working state for each ton of processed brown coal dust. Flow through the bottom is made so that at speed
    0 carrier gas at 0.025 m / s (normal load) at the bottom of the metering device, the pressure loss at the bottom is 0.2 bar. I. .
    The pipeline is transported
    5 a mixture of brown coal dust and a gas carrier (500 kg of brown coal dust for every 1 m of carrier gas in the working state, or 15.5 kg / m in the normal state). Pipeline
    0 is designed for the speed of a mixture of dust with a carrier gas of 3.4 m / s.
    Ii. According to the variant shown in Figures 1 and 3, two lock vessels are used to feed the dispenser 7.
    5 3 and 21 high pressure, alternating.
    Brown coal dust (properties are similar to pshi according to the variant shown on
    five.
    FIG. D and 2) is supplied to the spare bin 2. The spare bunker 2 is connected to the high pressure lock vessel 5 through a pipeline and a detent organ 4 and is connected to a high pressure lock vessel 21 through another pipeline and a stop valve 20. When the valve body 20 is closed, first, as in option I, the pressure in the lock vessel 5 is reduced, the latter is filled with brown coal dust from the storage bin 2 and through the regulating valve 14 with an inert gas through the pipeline 28 is brought to a pressure equal to the pressure in the dosing unit. During these processes, a pressure vessel 21 is opened through an open shut-off valve 22 and a coarse-dose device 23, which is under pressure and is made in the form of a cell drum with an adjustable speed, is connected to the metering device 7. At the same time, the contents of the high-pressure lock vessel 21 through the coarse dispensing device 23 enter the dispenser 7, the device 23 being controlled by the level gauge 17 so that within the specified limits the level in the dispenser 7 is kept constant.
    If the high pressure lock vessel 21 is empty, the level gauge 27 gives a signal that causes the valve 6 to open and the valve 22 to close. Then the brown coal dust from the high pressure lock vessel 5 is fed to the dispenser 7, while in the high pressure vessel 21, valve 26 decreases pressure. After opening the shut-off member 20, the high-pressure vessel 21 is filled with lignite dust. After receiving the signal of the maximum level of the level 27a, the shut-off body 20 is closed, through the regulating valve 25 with an inert gas, the high-pressure vessel 21 is adjusted to the pressure equal to the pressure in the dispenser 7, and, consequently, the level gauge 18 on the high-pressure vessel 21 is ready for the next discharge into the metering device 7. The operation of the metering unit and the supply of dust to the gasification reactor according to options I and II are similar.
    67194 b
    Two sluice locks: high-pressure vessels allow to reduce the level fluctuations in the dispenser 7, which increases the accuracy of the dosage 5 and reduces the size, especially: but the diameter, of the dispenser. Therefore, this design is advisable especially at high power settings.
    Iii. Device variant (FIG. 4
    O and 5) using only one metering device, some separate and regulated burners of one gasification reactor are supplied with pulverized fuel.
    5 Bottom part 8 of the dispenser 7 section. The Lena has three star-spaced dividing walls 38 for three identical sector plots. These plots are relative to
    0 to the upper part of the dispenser are open j so that the pulverized fuel from the upper part can flow freely into the lower part. The dividing walls also separate the flow day ;;
    5 24 and the intermediate space between the flow bottom and the outer wall of the bottom of the lower part. Each formed by the partition of the partition of the lower asti
    0 under the flow bottom has a supply for cenapaTlio of a controlled carrier gas injection, which flows through the flow bottom through the head amp &amp; that weight in the corresponding portion of the lower part and releases it to form partial fluidized beds. In each of these sections, a vertical pipeline 9 is terminated from above.
    Q for venting the carrier gas and the dust flow to each respectively attached burner 30 of the reactor 31.
    In this variant, the flow of dust is regulated mainly by means of measuring points 16 for drawing flow in separate transporting lines 9, the readings of which affect the installation valves 10 in the respective lines
    0 carrier gas supply, podpodshi in before. the congestion and the further course of the process in the gasification reactor are similar to those described.
    ,
    The use of the proposed installation for gasification of brown coal dust provides the following performance indicators: Fuel-brown coal dust
    17
    Grinding,% residue on a 0.2 mm sieve
    Moisture content,% 10 Ash content,% 10 Calorific value, kcal / kg 4950 Fuel consumption,. t / h 10 Working pressure, bar 30 Requirement for inert gas for pressure abor in sluice pressure vessel
    Pressure bar35
    Amount of gas, in normal condition750
    The need for carrier gas Pressure, bar35
    Amount of gas, m / h in normal condition
    The need for technical oxygen for gasification (96% Oj) m / h in normal condition 3680 The need for steam for gasification, t / h 1.85
    116719418
    The table shows the calorific value and yield of the carrier gas in the normal state.
    Carrier gas
    Nitrogen Uncleaned
    2400 own gas
    2500 14000
    13200
    The composition of the crude gas (dry),%
    CO52.2 54.5
    Hj31.0 32.3
    11.3
    WITH,
    11.8
    0.4
    sn
    0.4
    5.1
    1.1
    Prg is known for invention according to the results of the examination carried out by the Office for the Invention of the German Democratic Republic.
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    26
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    权利要求:
    Claims (14)
    [1]
    1. The method of gasification of pulverized fuels under pressure, preferably at a pressure of 5-50 bar, partial oxidation with oxygen or with a gasification medium containing free oxygen in a volatile cloud, and the pulverized fuel is brought to a pressure by means of a pressurized pressure vessel by means of a gaseous auxiliary medium • the gasification system and is led • to the dispenser, into the lower part of which pulverized fuel flows in the form of a quasi-quiet granular mass, where it is by blowing gaseous The medium, for example, the carrier gas, is loosened and, through the carrier pipe protruding into the lower part of the dispenser, is supplied to the burner or burners of the gasification reactor by means of the carrier gas stream, characterized in that the carrier gas stream supplied to the lower part of the dispenser after separate places of loosening of the pulverized fuel located in the lower part or the formation of a partial fluidized bed are divided into a first partial stream saturated with pulverized fuels and flowing to the burner or burners through the transporting pipeline of the gasification reactor, and the second partial stream flowing the entire height of the granular mass of pulverized fuel in the dispenser, the ratio of the saturation of the pulverized fuel to the volume of the first partial flow in the working state in the conveying pipeline is more than 300 kg / m 3 , the volume of the second partial flow corresponds to the volume of solid particles discharged from the batcher through the conveying pipeline the amount of dust, the ratio of the cross-section in the light of the conveying pipeline to s the free cross section of the crumbled part of the granular mass or partial fluidized bed is selected (1:50) (1: 300), the flow of dust flowing to the burner of the reactor is controlled by changing the amount of gas carrier flow supplied for loosening or swirling, and the pulse is The regulation of the dust flowing to the burner is obtained by direct measurement of the dust flowing to the burner or by measuring the quantity established in the gasification reactor. depending on the dust flow or on the relation of the dust flow to the amount of oxygen flowing to the burner per unit time.
    [2]
    2. The method according to claim 1, characterized in that the alternating operation of several, preferably two, lock pressure vessels connected in front of the dispenser is performed in such a way that at least one lock channel is continuously or excluding short switching periods, up to 10% of the total time high pressure to ensure unloading connected to the dispenser.
    [3]
    3. The method according to PP. 1 and 2, which includes the fact that the discharge of the sluice vessel or pressure vessels into the dispenser is carried out through a coarse dosage device or through an adjustable throttle device for dust flow, moreover, as a coarse dosage device or adjustable throttle device, it is used, for example, durable with squeezing a capsular cell drum, a dosing screw for coarse dosing or gates and using a known method of measuring the filling level in the dispenser by applying a control pulse to the device roughly dosage or throttling device is made so that the level within a certain range in the dispenser remains constant.
    [4]
    4. The method according to PP. 1-3, which includes the fact that in order to build up pressure in the sluice or pressure vessels and as a carrier gas, technical nitrogen or a mixture of nitrogen with air with an oxygen content of less than 6%, technical carbon dioxide, and combustible gas of foreign production are used , self-produced reverse combustible gas obtained by this method, or a mixture thereof.
    [5]
    5. The method according to PP. 1-3, characterized in that the pressure in the sluice or pressure vessels is inert gas, such as nitrogen, with a maximum oxygen content of 6% and / or technical carbon dioxide, combustible gas is used as the carrier gas.
    [6]
    6. The method according to PP. 1-3, characterized in that the pressure in the airlock or pressure vessels is carried out by an inert gas, such as nitrogen, with a maximum oxygen content of 6% and / or technical carbon dioxide, air or mixtures are used as the carrier gas inert gas oxygen with a maximum oxygen content of up to 21%.
    [7]
    7. The method according to PP. 1-6, characterized in that as a pulverized fuel used is dried, crushed to a grain size of preferably less than 0.5 mm and with a moisture content of up to 12% brown coal, the speed of the carrier gas in a free section in the lower 'part of the dispenser , is 0.0050.025 m / s, and the speed of the gas-carrier dust mixture in the conveying pipeline from the bottom of the dispenser to the burner is 1.0-7.0 m / s.
    [8]
    8. Device for gasification of pulverized fuels under. characterized by the fact that the dispenser consists of a shaft-shaped upper part, preferably of circular, log section, and of a lower part open with respect to the shaft-shaped upper part, or several lower parts open with respect to the upper shaft-shaped part, or of one open with respect to the upper shaft-shaped parts and into several sections of the divided lower part, the lower part or each of the lower parts, or each section of the lower part having a flowing bottom, which has at least one connection for flow regulated input of one gaseous medium, while in his or their inner space. through the side wall or through the flowing bottom or the shaft-shaped upper part of the dispenser, one or several pipes serving the conveyor pipe protrude, which are connected to the burner or burners of the gasification reactor.
    ,
    [9]
    9. The device according to p. 8, characterized in that the lower part of the dispenser has a smaller section than the shaft-shaped upper part, fitting the section of the upper part to the section of the lower part or parts, or to the section of the divided sections of the lower part is carried out so that located in the upper parts of the dispenser, the bulk mass of pulverized fuel slides down the cross section evenly and without the formation of funnels in the lower part or parts, or in divided sections of the lower part of the dispenser.
    [10]
    10. The device according to paragraphs. 8 and 9, characterized in that the flowing bottom under the temperature conditions provided for the carrier gas and pressure velocities from 0.005 to 0.025 m / s has an associated pressure loss over the entire cross section of the bottom, equal or greater than the product of bulk density and height granular mass of pulverized fuel in the dispenser.
    [11]
    11. The device according to paragraphs. 8-10, characterized in that in the line for supplying pulverized fuel to the metering unit for the dust flow, a known coarse dosage device or an adjustable throttle device is installed and supply over it. a coarse metering device or branches above an adjustable throttle device so that two or more high-pressure airlock vessels can be alternately unloaded into the dispenser, the upper part of the dispenser is equipped with a known level measuring device, which is connected via the corresponding regulator to the coarse metering device or throttle device, and the cycle times for reducing pressure, filling, pressurizing and unloading the pressure locks are consistent with each other, so that constantly and whether, excluding short switching periods, at least 10% of the total time, at least one high-pressure lock vessel is connected via a coarse dosage device or an adjustable throttle device to the dispenser to ensure unloading.
    [12]
    12. The device according to claim 11, wherein the high-pressure lock vessels have corresponding known filling level measuring devices that affect the adjustment of the high-pressure lock vessels, so that when the minimum filling level and the zero level are indicated, it is empty in one connected to the dispenser for unloading with the batcher, the pressure vessel lock is provided for switching to another pressure vessel filled with pulverized fuel and pressurized.
    [13]
    13. The device according to paragraphs. 8-12, characterized in that in the conveying pipeline or pipelines going from the lower part or lower parts, or from the divided sections of the lower part of the dispenser to the burner or gas burners of the gasification reactor, there are known measuring devices that flow to the burner, which act through the regulator to installation fittings or fittings in the inlet or inlets of carrier gas to pro. exact bottom or flow bottoms.
    [14]
    14. The device according to PP, 8-12, characterized in that the measuring device of the gasification installed in the reactor depends on the dust flow or on the ratio of the dust flow to the amount of oxygen supplied to the burner per unit time, preferably the temperature in the reaction space of the reactor, through the regulator to mounting valves or fittings in the inlet or inlets, for carrier gas to the flow-through bottom or flow-through bottoms.
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    同族专利:
    公开号 | 公开日
    PL209688A1|1979-06-18|
    YU42038B|1988-04-30|
    TR20754A|1982-06-24|
    DE2831208A1|1979-03-29|
    ATA524278A|1984-11-15|
    PL111707B1|1980-09-30|
    JPS5499103A|1979-08-04|
    AT378199B|1985-06-25|
    GB2004993A|1979-04-11|
    AU3989778A|1980-03-20|
    GB2004993B|1982-03-31|
    DD147188A3|1981-03-25|
    AU520077B2|1982-01-14|
    FR2403377A1|1979-04-13|
    HU180684B|1983-04-29|
    GR65885B|1980-12-01|
    YU220078A|1982-08-31|
    FR2403377B1|1985-01-25|
    CS222955B1|1983-08-26|
    IN150296B|1982-09-04|
    DE2831208C2|1988-01-14|
    YU111182A|1984-02-29|
    JPS594476B2|1984-01-30|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DD20106477A|DD147188A3|1977-09-19|1977-09-19|METHOD AND DEVICE FOR PRESSURE GASIFICATION OF DUST-SOUND FUELS|
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