• 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 concerns a method for the operation of gasification plants for pulverized fuels, wherein the pulverized fuel is reacted in a flame reaction with a gasifying agent containing free oxygen, into a combustible gas containing CO and H2. The task consists in precluding upon malfunctions in the supply of fuel, an oxygen discharge into the cooling and treatment plants, taking into consideration delays in the emergency shut-off systems and the controls for the oxygen supply. As per invention, a well-flowing additional fuel is stored in a reservoir at a pressure higher than the operating pressure of the gasification reactor. Upon malfunctions in the fuel supply, the additionally stored fuel will be transferred, within a short time, into the reaction chamber of the gasification plant. As additional well-flowing fuel combustible gas, liquid fuel or a pulverized solid fuel, also well-flowing, can be used.
    公开号:SU981348A1
    申请号:SU797770562
    申请日:1979-05-07
    公开日:1982-12-15
    发明作者:Петер Гелер；Петер Яшке；Хорст Кретцшмар；Клаус Кулбродт；Клаус Лукас；Бертхольд Неуманн；Манфред ШИНГНИТЦ；Ханс-Еахим Швейгель；Фридрих Бергер；Дитер Кениг
    申请人:Бреннстоффинститут Фрейберг (Инопредприятие)；
    IPC主号:
    专利说明:

    one
    The invention relates to a method of operating plants for the gasification of pulverized fuels, in particular to improve the safety of installations in emergency situations.
    In a technique for producing synthesis gas, reducing gas, heating gas and utility gas from solid fuels, a sensible solution is gasification of the fuel in a pulverized state by mastic oxidation. In the process of gasification, the pulverized fuel reacts with blast containing free oxygen at normal pressure or at elevated pressure in the temperature range from 1 ° C to 1 ° C ° C, with predominant formation of CO and Hj. The gasification process is carried out in an empty reaction chamber, and the average residence time of the fuel or the gas produced from it in the hot reaction chamber reaches about 0.5
    10 s. The blast is a mixture of technical oxygen and water vapor, and the proportion of technical oxygen fluctuates between 60-95%, depending on the fuel and the purpose of the produced gas. The process, in particular, maintaining the optimum temperatures in the reaction chamber, is controlled by regulating Q or the ratio of technical oxygen to dusty fuel, and the deviation from the given value of the weight ratio of oxygen to fuel by 10 can lead to changes in temperature, j ry in the reaction chamber by 200 K.
    During operation of the plant, due to gasification in the event of a fuel supply failure, especially when the consumption of pulverized fuel is reduced, the temperature in the reaction chamber rises to such a value that the technical safety of the plant is violated.
    that the ratio of oxygen to fuel exceeds the stoichiometric values required for complete combustion, or if the supply of pulverized fuel is completely stopped, excess oxygen for a few seconds {interacts with the CO and H obtained in the gasification process, in the hot reaction chamber. If the oxygen supply is not reliably shut off, the temperature in the reaction chamber will begin to decrease, but there is a danger that within a few seconds unreacted free oxygen from the hot reaction chamber will flow into the connected cooling and treatment units of the produced gas, which will lead to the formation there of explosive mixtures of oxygen and the resulting combustible hydrogen-containing gas will cause dangerous explosions. In order to prevent such difficult situations, the installations for the gasification of pulverized fuel are equipped with automatic emergency shutdown devices that reliably shut off the oxygen supply and switch the installation to a safe mode, in particular with an underestimated consumption of pulverized fuel in comparison with the specified flow rate and an overestimated oxygen consumption. as compared with a given flow rate and when the temperature in the reaction chamber is outside the specified limits, i.e., towards overestimation and understatement Aryan shutdown is inevitably struck by dead time, depending on the dead time of the measured data and on the duration of the closure of the shut-off means for the oxygen flow. In the case of high-power installations, this closure time can be several seconds and significantly affects .I1. I) a total dead time. Despite the duration of the closure and in the event of a sudden cut-off of the supply of pulverized fuel, protection against oxygen entering the cooling units is achieved when the ratio of the amount of oxygen supplied per unit of time to the amount of CO and H, 2 that is in normal condition in the reactor, is quite small and provides satisfactory recirculation in the reactor itself, however, this solution leads to a low specific productivity of the reactor.
    and therefore to too large reactor sizes.
    权利要求:
    Claims (2)
    [1]
    Another well-known solution involves the separation of the reaction chamber 10 15 I 5 1 several areas operated in. significantly independently of each other, each section having its own fuel supply system and blowing, and in an emergency case, the unreacted oxygen remaining in one of the sections can interact with the gas obtained in other parts of the reaction chamber, which prevents it from entering the cold parts installation. This solution requires sophisticated hardware design. The purpose of the invention is to create a method for operating gasification systems for pulverized fuel, which prevents the danger of oxygen entering the cooling and processing units of the produced gas if the supply of pulverized fuel to the reactor is disrupted, in particular in the event of a sudden interruption of this feed. The invention is based on the task of creating a method of operating gasification systems for pulverized fuel, which prevents the danger of oxygen entering the cooling and processing units of the produced gas if the supply of pulverized fuel to the reactor is disrupted, in particular when the feed is suddenly stopped, taking into account the final shutdown duration available oxygen shut-off means allowing high specific loadings of the reaction chamber and suitable for high capacity plants. According to the invention, the task is solved as follows. The additional tank contains fuel of good flowability or fluidity under pressure exceeding the operating pressure of the reactor. With the help of a pipeline disconnected in normal operation by means of automatically controlled shut-off means, additional fuel of good flowability when opening shut-off means is supplied to the reaction chamber near the place or points of oxygen or oxygen containing oxygen blowing If the supply of pulverized fuel to the reaction chamber fails at the same time emergency shutdown system in the reaction chamber with the automatic opening of auxiliary equipment is introduced due to the existing difference detecting stored in the auxiliary fuel tank good flowability or fluidity. The addition of good flowability to the reactor due to the high temperatures present in the reaction chamber interacts with the oxygen entering the reaction chamber until the automatic shutdown is fully triggered and thus prevents the oxygen from entering the cooling units. According to the invention, the pressure and volume of the tank, as well as the hydraulic resistance of the part connecting the tank and the reaction chamber, are consistent with each other so that the amount of additional fuel of good flowability entering the reaction chamber during the period from activation of the emergency shutdown system to full stopping the supply of oxygen to the reactor, exceeds the amount of fuel stoichiometrically necessary for complete binding of the incoming oxygen. There are no additional requirements for the amount of this additional fuel. In the solution according to the invention, depending on the type of additional fuel of good flowability or pressure in the tank, it is necessary to use pipelines connecting the tank and the reaction chamber with cross sections for which the opening time of the shut-off means in the connecting pipe is small compared with the duration closing the closure means in the oxygen supply line. In accordance with the capacity V of conventional shut-off valves and the maximum value of the pressure difference between the tank and the reaction chamber during the activation of the emergency shutdown system, when the shut-off valve starts up slightly, a large amount of additional fuel is moved relative to the maximum flow rate significantly reduced shortly before reaching the extreme position of the valves for supplying oxygen. In the method, a combustible, possibly high-calorific, gas from own production or other origin, such as natural gas, is preferably used as an additional fuel of good flowability. Liquid fuel can be used as a good flowability fuel, and the required pressure in the tank is provided by the vapor pressure of the liquid fuel or by the buoyer through inert or combustible gases. When using liquid fuels, it is recommended to use fuels that have good fluidity at ambient temperature and are not prone to the formation of tar or other solid precipitates. The need for additional fuel of the base is very small compared to the production volume of the plant. The economics of using high quality and expensive fuels for this purpose. When using medium or heavy heating oils as fuel of good flowability, the installation must be equipped with heating. . B, as well as additional fuel of good flowability, dusty solid fuel of choropey can be used, and a vessel is used as a reservoir for additional fuel, the pressure of which, due to the use of inert or combustible gas, exceeds the operating pressure in the reactor. The specified vessel is preferably located above the reactor inlet. and the principle of such a vessel is known from the field of pneumatic conveying. The pulverized fuel used for this purpose can be identical and the pulverized fuel used as a working fuel. However, in order to achieve improved fluidity, it may also be a fraction obtained from the main fuel by an additional enrichment measure, such as sifting or air separation, or it may be obtained by a separate enrichment process, especially suitable for achieving good fluidity. In order to use the invention, it does not matter in what form and by what means the pulverized fuel is supplied to the burner or to the burners of the gasification reactor under the normal mode of ex-, operation. It is advisable to use the invention in that case, when simultaneously with pulverized fuel, other flowing fuels that interact with the free oxygen-containing blast with the formation of gas containing CO and H are fed into the gasification reactor. The invention can be used, in particular the case when the pulverized fuel is supplied to the gasification reactor as a suspension in the liquid fuel, for example, in the heating fuel; oil or resin. FIG. Figure 1 shows a scheme for carrying out a method in which combustible gas is used as an additional good flowability fuel; in fig. 2 is a flow chart of a method in which brown coal dust is used as an additional pulverized fuel of good fluidity. Example 1. A reactor for gasification of pulverized fuel 1 at an operating pressure of 2.5 MPa is designed to produce 50,000 nm of raw gas per hour. Dust fuel in the form of a dense suspension in an inert carrier gas, technical oxygen and water vapor are introduced into the reaction chamber through the mount 2 located in the upper part of the reactor, and the three streams are mixed immediately after leaving the burner inside the reaction chamber The need for technical oxygen is | 14000 nm per hour; this corresponds to the amount of pure oxygen nm per hour or 3.7 nm per second with a purity of technical oxygen in the amount of 9b. The reactor is equipped with an automatic emergency shutdown system 3. Dead time from the moment of failure in the fuel supply (lowering the lower limit value) indicated by the measuring device - the amount of dust k, before the start of the shutdown process, is 7 sec. After the next 5 seconds, the oxygen supply is completely stopped by valve 5. During the first stage of dead time, 26 nm of oxygen are supplied to the reactor, during the second stage, due to the duration of closing of the shut-off valve for oxygen, 15 nm oxygen is supplied (on average,% normal flow). The installation according to the invention is equipped with a pressure vessel 6, in which methane (p) natural gas is stored under a pressure of 3.2 MPa. g ts The pressure tank is connected via a pipe to the inlet of the water vapor torch 2. When an emergency shutdown is triggered, an automatic emergency shutdown system 3 opens valve 7 and natural gas from tank 6 enters reactor 1 before pressure equalization. The capacity of tank 6 is 6 m, so that in an emergency shutdown, about 90 nm of natural gas enters the reactor. Natural gas interacts with the free oxygen that enters, with a maximum of 20.5 nm required for oxygen binding. Before starting up the gasification unit in operation in reservoir 6, it is necessary to increase the pressure by means of natural gas at a given value by means of compressor 8. Example 2. In this example, brown coal dust of good fluidity is used as additional fuel. Brown coal dust is stored in a pressure tank in the amount of 130 g in tank 6, and a pressure of 3.2 MPa is maintained by supplying nitrogen by means of a nitrogen compressor 8. The total capacity of the tank is 6 m, of which approximately 0.25 m is filled with dust. The pressure tank 6. is located above the burner 2 of the reactor 1 and is connected with a pipe to the inlet for coal dust of the burner
    [2]
    2. When an emergency shutdown is triggered by means of an automatic emergency shutdown system 3, a shut-off member 7 is opened, suitable for passing coal dust, and the nitrogen stored in tank 6 enters reactor 1 before pressure equalization, and the dust in tank 6 completely enters reactor 1 The dust interacts with the oxygen flowing into the reactor, and AO kg of dust is required to fully bind the stoichiometric oxygen. Prior to the commissioning of the installation, it should be ensured that the tank 6, in which atmospheric pressure is initially present, from the storage bin 9 is filled with the necessary amount of coal dust with subsequent pressure rise to 3.2 MPa with nitrogen. Claim 1. Instruction method for operating gasification systems for pulverized fuel in which pulverized fuel is supplied to. the reactor with the help of mechanical means or in a combustible or non-combustible gaseous or liquid medium in the form of a suspension and interacts with the blast containing free oxygen with a blow,
    the development of a combustible gas containing CO and I ,, oh l and h aa and the fact that, in an additional tank, fuel is stored of good flowability (or flowability pressure, exceeding the working pressure of the gasification reactor, and fuel stored in the tank, fuel of good bulk flow or flow for a short period of time is transferred to the reaction chamber of the gasification unit due to the pressure in the tank, input of the specified fuel of good flowability or flow into the reaction chamber py is performed near the place or places input containing free oxygen blow or stream containing free oxygen containing free blowing or blow oxygen streams, wherein the pressure vessel volume and flow resistance of the connecting portion between the reservoir and reaction chamber of the gasification reactor 981 are adapted to one ..
    ru for this period of time.
    2, the method according to claim 1, 1 and 2 with the fact that combustible gas is used as a good flow fuel, preferably a combustible gas with high heat of combustion.
    The method according to claim 1, wherein the liquid is used as a good flow fuel, and the pressure in the reservoir is created by the own vapor pressure of the liquid or by the supply of a combustible or inert gaseous medium. .
    A. The method according to claim 1, is also distinguished by the fact that pulverized solid fuel is used as a good flowability fuel and the pressure in the reservoir is created by supplying a combustible or inert gaseous medium.
    Recognized as an invention according to the results of the examination carried out by the Office of German Invention 810 with a friend so that the amount of good flowability fuel transferred to the reaction chamber in a short period of time from the start of the drive to freeze the disturbance until the free oxygen supply was completely stopped. bonding the free oxygen permeation into the reaction chamber of the Democratic Republic. you-- rt -J .1 r CHEIG xB4
    and
    Synthesis gas
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    同族专利:
    公开号 | 公开日
    TR20695A|1982-05-06|
    DE2917536C2|1987-01-08|
    US4325709A|1982-04-20|
    DE2917536A1|1979-12-06|
    CS223559B1|1983-10-28|
    FR2427379B1|1985-03-08|
    GB2022133A|1979-12-12|
    HU182457B|1984-01-30|
    DD136748B1|1980-10-01|
    PL215859A1|1980-02-25|
    FR2427379A1|1979-12-28|
    AT375670B|1984-08-27|
    DD136748A1|1979-07-25|
    ATA349579A|1984-01-15|
    IN153534B|1984-07-21|
    GB2022133B|1982-05-12|
    JPS54158405A|1979-12-14|
    AU4757479A|1979-12-06|
    YU126579A|1984-06-30|
    JPS5846237B2|1983-10-14|
    AU526706B2|1983-01-27|
    GR65513B|1980-09-17|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE524439C|1929-10-25|1931-05-12|Julius Pintsch Akt Ges|Process for the prevention of explosive mixtures during the production of combustible gases like generator gas from coal or coke dust|
    US2395384A|1943-05-25|1946-02-19|Askania Regulator Co|Pilot control for primary and secondary fuels|
    DE856188C|1947-12-29|1952-11-20|Koppers Co Inc|Process for the gasification of finely divided solid fuels in suspension with oxygen|
    DE1026031B|1952-02-18|1958-03-13|Koppers Gmbh Heinrich|Monitoring system for devices for the production of fuel gas from solid or liquid fuels|
    DE1137819B|1954-12-29|1962-10-11|Kloeckner Humboldt Deutz Ag|Process for regulating the fuel supply to a fluidized bed gas generator or to a floating gasifier|
    DE1023746B|1955-10-27|1958-02-06|Koppers Gmbh Heinrich|Process for the continuous generation of water gas|
    US2919980A|1957-10-22|1960-01-05|Koppers Co Inc|Apparatus for gasification of finely divided solid or liquid fuels|
    DE1125108B|1958-06-21|1962-03-08|Sumitomo Chemical Co|Process for the automatic control of the feed of the reactants to a coal dust suspension gasification device|
    US3159345A|1962-01-05|1964-12-01|Phillips Petroleum Co|Control system for utilization of variable flow fuel|
    US4017269A|1972-03-25|1977-04-12|Krupp-Koppers Gmbh|Method and arrangement for gasifying finely divided fluidized solid combustible material|
    US4017272A|1975-06-05|1977-04-12|Bamag Verfahrenstechnik Gmbh|Process for gasifying solid carbonaceous fuel|
    US4032287A|1975-06-16|1977-06-28|United States Steel Corporation|Combination burner|DE3823773A1|1988-07-14|1990-01-18|Krupp Koppers Gmbh|METHOD FOR DETERMINING AND CONTROLLING THE FUEL MASS CURRENT IN PARTIAL OXIDATIONOF FINE-GRAINED TO DUST-SHAPED FUELS|
    US20070011945A1|2005-07-05|2007-01-18|Gerard Grootveld|Systems and methods for producing synthesis gas|
    US7722690B2|2006-09-29|2010-05-25|Kellogg Brown & Root Llc|Methods for producing synthesis gas|
    US8888875B2|2006-12-28|2014-11-18|Kellogg Brown & Root Llc|Methods for feedstock pretreatment and transport to gasification|
    US9157043B2|2008-07-16|2015-10-13|Kellogg Brown & Root Llc|Systems and methods for producing substitute natural gas|
    US9132401B2|2008-07-16|2015-09-15|Kellog Brown & Root Llc|Systems and methods for producing substitute natural gas|
    US9157042B2|2008-07-16|2015-10-13|Kellogg Brown & Root Llc|Systems and methods for producing substitute natural gas|
    US7955403B2|2008-07-16|2011-06-07|Kellogg Brown & Root Llc|Systems and methods for producing substitute natural gas|
    CN101561449B|2009-05-27|2010-12-01|内蒙古科技大学|Anti-explosion powder supply device|
    US9133405B2|2010-12-30|2015-09-15|Kellogg Brown & Root Llc|Systems and methods for gasifying a feedstock|
    DE102011083850A1|2011-09-30|2013-04-04|Siemens Aktiengesellschaft|Pneumatic fuel supply from a metering vessel to a high differential pressure gasification reactor|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DD20567978A|DD136748B1|1978-05-31|1978-05-31|METHOD FOR OPERATING GASING SYSTEMS FOR DUST-SOUND FUELS|
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