• 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:
    A method for quenching cracked gases and recovery of heat therefrom by cooling the gases in heat exchange with steam to increase superheat level of the steam and subsequently recovering heat from the superheated steam.
    公开号:SU959631A3
    申请号:SU782675850
    申请日:1978-10-19
    公开日:1982-09-15
    发明作者:Патрик Эннис Бернард (Старший)；Ричард Стислингер Джеймс
    申请人:Пуллман Инкорпорейтед (Фирма)；
    IPC主号:
    专利说明:

            - -. .
    The invention relates to methodall
    cooling the cracked gases obtained during steam reforming of hydrocarbons in the production of olefins, and utilization of these gases.5
    A known method of cooling the cracking. -: gases obtained in high-temperature installations processing hydrocarbon raw materials by direct mixing them with a cooling liquid, ijqpea-fg, which is an oil cancer. boiling out) and 371-427С.
    Closest to the proposed method of cooling the cracking gases. on the pyrolysis process of carbohydrates in the presence of water vapor to obtain olefins by indirect heat exchange in a shell-and-tube heat exchanger followed by treatment of the product cooled by 45 0 5 with liquid high boilers 15) with thermal cracking products, after which the cooled product is introduced into one or several parallel operating heat exchangers of the second stage, where the temperature of the cracking of gases decreases -.
    with up to 35O-45O C. As a heat-mixing medium, 1fnmen to t water under high pressure, then used for generating your own steam water 2J.
    A disadvantage of the known methods is the low level of heat of crust: gas condensate and significant coking power.
    The purpose of the invention is to increase the approval level. akii heat cracks ggazov and reduction of coping.
    Delivered by the fact that according to the method of cooling the cracking gases during the process of cholysis of the carbohydrates of one raw material in the absence of water vapor with the production of olefins, indirect heat exchange with the cooling medium uses water vapor followed by cooling of the superheated steam obtained by direct heat exchange with water to produce pressurized steam.
    Steam parvolvza equipment is any tube furnace, which is suitable for cracking a single row of hydrocarbon fractions, such as ethane, propane, light naphtha boiling in the range of 32-121 ° C, naphtha of the whole range boiling in the range of 38-190 ° C, light gayoil, boiling range 176-, average gas oil boiling in the range of 232-454 ° C, heavy gas oil boiling in the range of 315-538 seconds, or their mixtures. With the particular design of the kiln, as a raw material for cracking, whole oil can be used. A conventional tubular kiln has one or a series of radiant sections containing tubes for high-temperature cracking, fired by a variety of gas or oil burners located in the walls, arch or hearth of the kiln. Usually, two or three cracking tubes are used, however, tube bundles can vary from one tube of larger diameter to bundles containing a plurality of tubes of small diameter. These pipes can be assembled together from the bb side to collect gases in one or several collectors for subsequent cooling or cracking pipes can be connected to shell-and-tube type cooling devices separate for each pipe. The temperature at the exit from the cracking pipes varies approximately in the range of O4-G1038s, depending on the choice of starting material, the required yields and the desired product mixture. The typical temperature at the outlet of the radiant tube, used when cracking from light to heavy gas oils, is in the range of about 7,04927 ° C. In addition, the tubular furnace must have one or a series of convection sections where the heat from the flue gases of the radiant burner is used to preheat the initial heat source for heating or superheating the steam used in turbine drives, for heating and as a dilution steam for pyrolysis. A suitable apparatus for use in the cooling zone is conventional shell-and-tube heat exchangers with one or a plurality of pipes, preferably one-way, designed for perceiving thermal gradients arising from high-temperature cracking gases. In one of the variants of the proposed method, saturated steam under pressure of 3.5-217 atmospheres enters the cooling zone to produce heat by indirect heat exchange with cracking gases at a temperature of approximately 7 ° 4–1038 ° C, and cools these gases to a temperature of approximately 260 ° C. 649 ° C for setting pyrolysis reactions. Then cr-; ing gases are fed to subsequent cooling stages in order to cause the cracking gas temperature to be even, at which normal gas products, such as olefins, hydrogen n C. paraffins, can be separated from normal liquids, such as pyrolysis gasoline and petroleum, and cracks -, king in the fractionation column of the pyrolyzed stream. These subsequent cooling stages can be shell-and-tube heat exchangers for additional utilization of low-temperature heat or direct oil cooling to extract low-temperature heat in the fractionating system of the effluent stream. The flow of saturated steam in the cooling zone in the preferred embodiment is associated with the flow of cracking gas in order to maintain a relatively constant temperature of the pipe wall along the entire length of the cooling zone. It is most preferable to maintain the wall temperature above the dew point of the cracking gas. The preferred use of the heat recovered in the cooling zone in the form of high-pressure steam is to drive the target gas and compress the refrigerant. With such heat utilization, the preferred Pressure Range of the saturated vapor cooler for the cooling zone is 15 and 3.5–217 Ata with an associated saturation temperature of about 240371 ° C. . in the cooling zone, steam superheat increases from 0 to at heat exchanger with hot cracking gases. This steam is then sent to the overheating zone, where it is subjected to indirect heat exchange with water at a slightly higher pressure, which is heated to the temperature of the sediment. In accordance with this, superheat is removed from the cooling steam supply, and heat is removed from the overheat relief superheat as saturated steam at elevated pressure, which can subsequently be used as a coolant feed to the cooling zone. Non-superheated steam leaving the overheating zone can be at the saturation temperature for the pressure used or can retain some superheat at about a temperature higher than the temperature of the saturated. This steam can be reheated again in the convection coil of the pyrolysis section or in a separate superheater for subsequent use as steam to drive the bin for the above-mentioned compression equipment. The temperature of the vapor leaving the overheating zone should be regulated in the region from the inlet temperature to the first cooling zone and then sent to the second cooling zone to cool the cracking gases from another radiant coil or pipe bundle in the same or in another the pyrolysis zone. The lost steam overheating is again superheated by indirect heat exchange with cracking gases in the BTqpog cooling zone, operating similarly to the first zone, and overheated steam under a pressure of 3.5-217 atmospheres is removed from the second cooling zone for use in steam turbine drives. The steam removed from the second cooling zone for use as steam turbine and in refrigeration compression equipment should be at a pressure of 3.5-217 atm and should have an overheating of approximately 93260s. When removing superheated steam in the above pressure range, the vapor pressure in the first cooling zone and the superheat removal zone is in the same range .., In cases where multiple cooling zones are used, for example, with limited steam availability, Can U) be called one or several intermediate cooling zones and superheat removal zones In the use case of, for example, one intermediate stage, the unheated steam leaving the superheat removal zone, passes successively through the intermediate cooling zone, y) intermediary deprotection overheating zone and then to the cooling zone. The saturated steam that is introduced into the overheating zones is removed, before its introduction as a refrigerant into the first cooling zone, is sent to a steam trap (of the preferred option). The preferred device for introducing Water from the steam trap into the overheating zone and extracting the steam from the steam trap is a conventional thermosyphon. In another embodiment of the proposed method, superheated steam of relatively low pressure is used as chidag | yy in the cooling zone. This option allows the use of a less durable cooling device design due to the use of more low vapor pressure in the case of using lower pipe wall temperatures, for example, when working with lightweight raw materials. In this embodiment, steam under pressure of 3.5-7 at. superheated to about 149-427 ° C, is introduced into the cooling zone, where the superheat is increased due to indirect heat exchange with the cracking gases. This steam is then sent to the superheat removal zone to extract the superheat due to indirect heat exchange with water at an elevated pressure to generate an elevated pressure steam of about 35-217 atmospheres. At elevated pressure, it may overheat in the convection coils of the Sh1I pyrolysis unit in a separate superheater and be used as steam to drive turbines. Non-superheated steam leaving the superheat zone at relatively low pressure can be used for process heating or can be reheated in convective coils of the pyrolysis section or by heat exchange with hot steam from the turbine for high pressure turbines for subsequent use. The low pressure vapor released from overheating exits the first overheating zone to the same temperature, for which the OH-gas enters the first Cooling zone, the second cooling zone, where it is reheated due to indirect heat exchange with the cracker-gas. The superheated low-pressure steam, which comes out of the second cooling zone, is again deprived of overheating in the second nejierpeBa withdrawal zone, where the amount of high-pressure steam additionally increases due to indirect pressure; heat exchange with water .. As in the first variant (s, the water used for high pressure pfa heating is preferably heated up to the tempo of the ature rate corresponding to the specific pressure chosen for the high pressure steam system. The heated water can pass through the steam collector and the loan is directed to the overheating zone through the circulation tubes of thermosions, the steam rises and then enters the steam tank. Saturated high-pressure steam from the steam tank is then superheated subchieveously in a convective tank. they are pyrolyzed and then disposed of as power oil for high pressure steam turbines. Example 1. Preheated source gas oil diluted with steam enters the pyrolysis zone when it is distributed to radiant coils, which are usually moved by fire oil burners installed in the radiant section of the pyrolysis zones. The feedstock is heated to the cracking temperature to produce olefins, normal liquids, hydrogen and methane. The cracking gases are directed to the cooling zones, where the cracking reactions stop as the gases cool down to indirect heat exchange with steam. The cooled gases leave the respective cooling zones and assembled. in a common collector for further cooling, compression and separation of the cracking of gases. Steam refrigerant is supplied successively to cooling zones, in which saturated steam is placed under a pressure of 1O5 ata, coming from napoc6qpHHKa. Fresh water for the steam trap is heated in a convection coil located in the upper part of the zone 1 of the hydrolysis, which enters the steam trap. Additionally, steam is supplied to the steam collector. The refrigerant in the form of saturated steam overheats up to 482 ° C and enters the overheating zone, where it cools down to 324 ° C due to indirect heat exchange with water from a thermo siphon. In the overheating zone, the heat is recovered in the form of steam under a pressure of 1015 at. In the steam trap, and the resulting high pressure steam enters the first cooling zone, as described above. The overheated steam leaves the overheating zone when it enters the second cooling zone, where it reheats up to 482 ° C. This steam under pressure of 105 atmospheres and leaves the second cooling zone and goes to high-pressure turbines, which serve to compress, 1X Cracks of gases and refrigerant used in the separation of separation and extraction of the target (Zhefinov. Example 2. The cooling and heat recovery system is the same as Example 1 except for the additional cooling cycle located between the first and second zones and cooling resulting in the formation of a three-way cooling system.The hot cracking gases from an additional radiant coil located in the pyrolysis zone enter the intermediate cooling zone and are cooled to 593 ° C due to indirect heat exchange with the steam leaving the zone overheat removal. This steam is reheated in the intermediate cooling zone and directed to the intermediate, exactly the superheat removal zone, which operates in the same way as the above described superheat removal zone. The superheated steam leaves the y) interim overheating zone with temperature and enters the second cooling zone, where it is again superheated to. Further, the process proceeds analogously to Example 1. Example 3. The cooling and heat recovery system also produces n high pressure, but medium pressure steam is used as the refrigerant in the cooling zones. The preheated feedstock (gas oil), diluted with steam, enters the pyrolysis zone at 53 ° C and is distributed to radiant coils, which are usually heated by fire from burners located in the radiant section of the Olis area. The hot cracking gases from the radiant coils enter the cooling zones, where the cracking reactions stop due to the cooling of the gases before indirect heat exchange with steam. The cooled gases exit the respective cooling zones and collect in a common manifold for further cooling, compression and separation of the cracking of gases. Steam refrigerant is successively supplied to the cooling zones, where superheated steam enters at 45.5 atm. This steam comes out of the turbines with a vapor pressure of 1O5 atm in the form of exhaust steam at a pressure of 45.5 atha and a temperature of 9090s. The exhaust steam is cooled to a steam-cooling turbine before it enters the first cooling zone.
    The steam refrigerant is superheated before, after overheating, enters the first cooling zone, where it is cooled prior to indirect heat exchange with water to a thermosyphon in the zone, the heat in the zone is discharged as a saturated, direct OO steam vapor. Fresh water is supplied to the steam collector at a pressure of 105 atm and is heated in a convective coil located in the upper part of the zone and is directed to the drum. Additional 1st steam is fed into the drum.
    After overheating, the hot-melted steam leaves the first cooling zone and then goes to the second one, where it re-heats, from to. This steam leaves the second cooling zone and is cooled again after overheating in the second removal zone, overheating to Z29c by indirect heat exchange with water from a thermosyphon. The superheated steam leaving the second cooling zone is again superheated in the steam turbine's desuperheater with exhaust steam from high-pressure turbines V and is used as a steam of 45.5 atm to drive medium-pressure turbines.
    Saturated steam is pumped by the 1O5at to the steam collector due to the operation of 30 thermosyphons. This steam comes out of the bar.
    A ban is placed in a steam reheat coil located in the pyrolysis section of the pyrolysis, and then goes to high-pressure turbines 1O5 ata, which serve to compress the cooled roll gas and refrigerant used to separate and extract the target olefins.
    formula and. 3 gains
    The method of cooling the cracking ges of the process of schfolysis of utevodorsdns h) raw material for the absence of water steam & with olefins via indirect heat exchange with a cooling medium, characterized in that, with a chain of efficient utilization of test cracking gas and reducing coke accumulation, water and K asp are used, followed by cooling of the heated superheated steam by means of a heat medium. with getting naru voyoeshyugo pressure. Source information. taken into consideration pr expertise
    1. Pathey USA No 3676519, cl. 26O-683, published. 1972.
    2. US Patent No. 3593779, cl. 165-1, publ. 1971. (yurototil).
    权利要求:
    Claims (1)
    [1]
    Claim
    A method for cooling cracked gases of a pyrolysis process of hydrocarbon feedstock, in the presence of water vapor to produce olefins by indirect heat exchange.
    <with a cooling medium, characterized in that, in order to increase the efficiency of heat recovery of the cracking gases and reduce coke deposition, water pf is used as the cooling medium, followed by cooling of the resulting superheated steam by indirect heat exchange with water to produce steam. high blood pressure.
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    同族专利:
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    FR1277746A|1961-01-17|1961-12-01|Schmidt Sche Heissdampf|Method and device for cooling cracking gases|
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    US7404891B2|2004-03-29|2008-07-29|Exxonmobil Chemical Patents Inc.|Heat recovery technique for catalyst regenerator flue gas|
    US7488459B2|2004-05-21|2009-02-10|Exxonmobil Chemical Patents Inc.|Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking|
    US7763162B2|2005-07-08|2010-07-27|Exxonmobil Chemical Patents Inc.|Method for processing hydrocarbon pyrolysis effluent|
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    US8074973B2|2007-10-02|2011-12-13|Exxonmobil Chemical Patents Inc.|Method and apparatus for cooling pyrolysis effluent|
    US20090301935A1|2008-06-10|2009-12-10|Spicer David B|Process and Apparatus for Cooling Liquid Bottoms from Vapor-Liquid Separator by Heat Exchange with Feedstock During Steam Cracking of Hydrocarbon Feedstocks|
    US20120024749A1|2010-07-30|2012-02-02|Strack Robert D|Method For Processing Hydrocarbon Pyrolysis Effluent|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/843,462|US4107226A|1977-10-19|1977-10-19|Method for quenching cracked gases|
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