• 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:
    Improved performance is obtained in a multi-tube reactor for oxidation of ethylene to ethylene oxide by providing a distribution zone for the coolant located downstream of the catalyst and a contiguous cooling zone. The effluent gases from the oxidation are cooled in the cooling zone by a fluid, which has been only slightly preheated and distributed uniformly in the distribution zone by contact with tubes in which the effluent gases are in low-turbulence flow. Uniform distribution of the coolant provides substantially equal cooling of the effluent gases in each tube, thus minimizing the variation in effluent gas temperature among the tubes. Preferably, the tubes in the cooling section are packed with inert particles to facilitate heat transfer, while the tubes are empty in the distribution section to reduce heat transfer.
    公开号:SU1637657A3
    申请号:SU843754457
    申请日:1984-06-29
    公开日:1991-03-23
    发明作者:Дж.Озеро Брайан；Д.Бекер Стенли
    申请人:Дзе Халкон Сд Груп Инк (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to the structural design of tubular reactors for carrying out exothermic chemical reactions, in particular for carrying out a catalytic oxidation of ethylene to ethylene oxide in it.
    The aim of the invention is to reduce the heat transfer process by providing a low-turbulent regime.
    Fig, 1 shows schematically a reactor; FIG. 2 is a graph of the reactor operating characteristics.
    Reactor 1 contains tubes 2. Each tube is sealed in the form of inlet 3 and outlet 4 tube sheets. The internal baffles 5 and 6 divide the lower part of the shell into distribution and cooling zones. The baffle 5 and the outlet tube 4 define a zone
    distribution, and the baffle baffle 5 and the baffle baffle 6 - the cooling zone. Water for feeding the boilers, having a temperature of 168 ° C, is supplied to the distribution zone through conduit 7 where it is distributed with minimal heating so that water vapor passes through a circular opening in the baffle wall 5. where each tube passes through the partition Outer diameter the tube is 38.1 mm and the hole diameter is about 38.9 mm5, which is enough to create the necessary uniform distribution of water to power the boilers.
    Water flows upward, mainly in a laminar flow regime, adjacent to the tube with which it interacts, receiving heat to raise the temperature almost to the boiling point.
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    O5
    SD
    s

    s
    A main recirculation wave for feeding the boilers is fed above the baffle wall 6 to the main heat sink section limited by the inlet tube 3 and the baffle wall 6 where water boils and is discharged as steam through pipe 8. Each tube is 10.6 m long 8 m filled with a silver catalyst on a carrier, having a 6-8 mm substrate, which is calibrated to ensure good contact, but without unduly restricting the flow of gases passing through the tube. The preheat zone is approximately 0–6 m long, which may vary with the water level on the outside tube side. The heating is applied to feed gases in an area that is compacted with an inert material, similar to that used as a catalyst carrier.
    The cooling zone between the baffles 5 and 6. has a length. 1.5 m, and the tubes are filled with inert particles, which are used for heating. The purpose of incorporating inert material into both zones is to facilitate heat transfer to or from liquids passing on the outside tube side, i.e. In order to obtain heat from steam in the preheating zone and heat transfer to water for feeding the boilers in the cooling zone, it is preferable to leave each tube section extending into the distribution zone free from any inert material that should promote heat transfer. Any solid material in tube 2 should not disrupt the flow of gases to a large extent in order to obtain the desired microturbulence. The velocity of the gases inside the tubes slows down from 3 m / s as it passes through the spaces between the inert particles in the cooling zone to 1 m / s in the unfilled distribution zone. Therefore, the heat transfer coefficient is reduced by 90%.
    The water velocity for feeding the boilers on the off-pipe side of the distribution zone is also kept low (i.e., in low-turbulent flow in order to minimize heat transfer on the off-pipe side. Thus, the distribution zone
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    serves to separate the water to power the boilers into multiple water streams (one for each tube) that flow vertically into the cooling zone and cool the exhaust gases.
    The reactor in the oxidation of ethylene works as follows.
    Fresh raw materials containing ethylene and oxygen flows are directed through conduit 9 and are connected to recirculation gases in conduit 10 with a content,%: ethylene 15-30; oxygen 7-9; CO 5-15; Argon 5-15 with a balance of nitrogen and methane. The temperature and pressure of the combined feed stream are 180 ° C and 22 kg / cm2 gauge.
    The gases enter the open part above the inlet tube sheet 3 and pass into the tubes 2 of the reactor, where they are heated to a temperature of about 240 ° C. The reaction starts at the top of the reaction zone. The heat of reaction is removed by boiling Bonofij supported at a temperature of about 240 ° C and a gauge pressure of 34.5 kg / cm2 using pressure regulators (not shown). The flue gas temperature at the exit of the cooling zone (i.e., baffle plate 6) is 245 ° C.
    Gases pass down each tube 2 countercurrent to the water for feeding the boilers flowing upward from the distribution zone; thereby cooling the gases to 235 ° C with simultaneous heating of water for feeding the boilers to 240 C. The temperature of the exhaust gases varies by a very small amount from one tube to another, because the water flow is proportional to the gas flow and the water temperature can only rise to boiling point that limits heat transfer. The gases enter the distribution zone, where, due to the deliberately low heat transfer, further cooling to 0.3-3.5 ° C of the lower part of the tube 2 takes place.
    Water for feeding the boilers is proportional to the gas flow when passing through the circular holes between the pipes and the horizontal baffle 5. The temperature rises from 168 ° C to the inlet to 171 ° C near the shell and to 189 ° C in the center of the reactor. The gases are cooled almost equally. The gases exit each tube into the outlet of the reactor where they are mixed and then discharged through line 11 to reduce the ethylene oxide.
    The graph (Fig. 2) shows the operating characteristic of the proposed reactor as compared with the known one, characterized in that the tubes in the distribution zone are sealed with an inert material instead of being unfilled. The effect causes temperature fluctuations between the gas in the shell and on the centerline, equal to 14.3 ° C, compared with 3.8 ° C, when the tubes are empty. If the waste gases enter the distribution zone at 235 ° C, the gas in the tubes adjacent to the shell is cooled to 215 ° C, whereas in the tubes near the middle line, the temperature is 230 ° C.
    A large temperature difference is caused only by compaction in tubes located in the distribution zone, as a result of which an increase in heat transfer coefficient is highly undesirable. If a certain maximum temperature does not exceed, for example, 230 ° C, then the operating temperature in the reactor should be limited to a value of 10 ° C lower than the invention. The durability of the catalyst is shortened as the temperature cannot be increased as much as possible.
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    ra when he gets old. The reactor under 1 is largely a danger associated with excessively high tem peratures at the outlet, namely, production costs and potential damage to equipment.
    The indicated temperatures are typical for initial conditions of working with a fresh catalyst, comparative differences in temperatures will be found when the catalyst is aged. Since temperatures are on average higher at this time, the dangers become greater, and the proposed reactor has great advantages.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    A tubular reactor for carrying out exothermic chemical reactions in the vapor phase, comprising a housing inside of which tubes with gaps fixed for catalyst are fixed in tube plates with a gap, and a cooling chamber located below the bottom tube grid, in order to reduce the heat transfer process due to the provision of a low-turbulent regime, it is equipped with a distribution chamber placed under the cooling chamber and made in the form of a shell with two plates and tubes fixed in them is necessary in order to proti- GOVERNMENTAL coaxially with tubes zapolnenny10
    five
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    0
    ra when he gets old. The reactor is subjected to a large extent to the hazards associated with excessively high outlet temperatures, namely, production losses and potential destruction of equipment.
    The indicated temperatures are typical of initial operating conditions with a fresh catalyst, comparative differences in temperatures will be detected when the catalyst is aged. Since temperatures are on average higher at this time, the dangers become greater, and the proposed reactor has great advantages.
    Invention Formula
    A tubular reactor for carrying out exothermic chemical reactions in the vapor phase, comprising a housing within which tubes filled with a catalyst are fixed in tube plates with a gap, and a cooling chamber located under the lower tube sheet, characterized in that the heat transfer process is reduced by low-turbulent mode, it is equipped with a distribution chamber placed under the cooling chamber and made in the form of a shell with two plates and tubes fixed in them mi coaxially with tubes filled
    loss of catapizatom activity and catalyst.
    FIG. one
    ° С
    240
    230 220 210
    240,230
    220 210
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    IT986732B|1973-04-30|1975-01-30|Snam Progetti|PROCEDURE FOR CONDUCTING PARTIAL OXIDATION REACTIONS WITH OXY GENO OF ORGANIC COMPOUNDS IN THE STEAM PHASE AND EQUIPMENT SUITABLE TO CARRY OUT THIS PROCEDURE|
    US4061659A|1976-06-28|1977-12-06|Shell Oil Company|Process for the production of ethylene oxide|
    JPS6045637B2|1978-07-26|1985-10-11|Nippon Shokubai Kagaku Kogyo Kk|
    DE3028646C2|1980-07-29|1989-01-19|Metallgesellschaft Ag, 6000 Frankfurt, De|DE3631642A1|1986-09-17|1988-04-07|Linde Ag|METHOD FOR CARRYING OUT CATALYTIC REACTIONS|
    JP2778878B2|1991-09-12|1998-07-23|株式会社日本触媒|Method for producing ethylene oxide|
    DE19719375A1|1997-05-07|1998-11-12|Linde Ag|Process and reactor for producing ethylene oxide|
    JP4499219B2|1999-10-04|2010-07-07|株式会社日本触媒|Method for producing ethylene oxide|
    EP2231324B1|2007-12-18|2016-06-29|Dow Technology Investments LLC|Tube reactor|
    WO2021010851A1|2019-07-12|2021-01-21|Mladen Milinkovic|Durable construction object made of three layered prefabricated ferocement constructive elements|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US50969583A| true| 1983-06-30|1983-06-30|
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