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    • 1. 发明申请
    • PROCESS FOR THE TREATMENT OF LIGHT NAPHTHA HYDROCARBON STREAMS
    • 用于处理轻质石墨烃流程的方法
    • WO1998012158A1
    • 1998-03-26
    • PCT/US1997015133
    • 1997-08-28
    • CHEMICAL RESEARCH & LICENSING COMPANY
    • CHEMICAL RESEARCH & LICENSING COMPANYHEARN, DennisGILDERT, Gary, R.
    • C07C05/00
    • C10G65/06C10G2300/4087Y10S203/06
    • A process for treating a light cracked naphtha (1) to be used as an etherification or alkylation feedstock in which the mercaptans and diolefins react in a single pass fixed bed reactor (20) and are removed in a distillation column reactor (10) which hydrogenate the unreacted diolefins. The mercaptans are reacted with the diolefins to form sulfides which are higher boiling than that portion of the naphtha which is used as feed to the etherification or alkylation unit. The higher boiling sulfides are removed as bottoms along with any C6 and heavier materials. Any diolefins not converted to sulfides are selectively hydrogenated to mono-olefins for use in the etherification process. Certain C5 olefins, for example pentene-1 and 3-methyl butene-1 are isomerized during the process to more beneficial isomers.
    • 一种用于处理轻度裂化石脑油(1)的方法,其用作醚化或烷基化原料,其中硫醇和二烯烃在单程固定床反应器(20)中反应,并在蒸馏塔反应器(10)中除去,氢气化 未反应的二烯烃。 硫醇与二烯烃反应形成沸点高于用作醚化或烷基化单元的进料的石脑油部分的硫化物。 较高沸点的硫化物作为底部以及任何C6和较重的材料被除去。 任何未转化成硫化物的二烯烃都被选择性氢化成单烯烃,用于醚化过程。 某些C5烯烃,例如戊烯-1和3-甲基丁烯-1在该过程中被异构化为更有益的异构体。
    • 6. 发明申请
    • ETHERIFICATION-HYDROGENATION PROCESS
    • 加氢加氢过程
    • WO1997028874A1
    • 1997-08-14
    • PCT/US1996020896
    • 1996-12-31
    • CHEMICAL RESEARCH & LICENSING COMPANY
    • CHEMICAL RESEARCH & LICENSING COMPANYHEARN, DennisGILDERT, Gary, R.GROTEN, Willibrord, A.
    • B01D03/34
    • B01D3/009C07C41/06C07C41/42Y02P20/127Y10S203/06C07C43/046
    • A process for removing dienes from etherification uses a hydrogenation zone (24) in the reactor distillation column (20) above the etherification zone (22). MTBE is produced and the unreacted C4 stream is also subjected to selected hydrogenation of the butadiene contained in the C4 feed stream. The C4 stream is introduced via line (101) and methanol is introduced via line (102) which is combined in flow line (104) and subsequently enters the distillation column (20) via line (103) wherein the C4 stream is contacted with methanol in the etherification zone (22) where the MTBE is distilled downward. The unreacted C4's then are subjected to selective hydrogenation in the hydrogenation zone (24) wherein butadiene in the overhead raffinate (108) is reduced by over 90 %. The hydrotreated C4's are thus suitable for cold acid alkylation or other use wherein butadiene is harmful.
    • 用于从醚化中除去二烯的方法在醚化区(22)上方的反应器蒸馏塔(20)中使用氢化区(24)。 生产MTBE,并且还对未反应的C4物流进行C4进料流中包含的丁二烯的选择氢化。 经由管线(101)引入C4流,并且经由管线(102)引入甲醇,该管线(102)在流动管线(104)中组合,随后通过管线(103)进入蒸馏塔(20),其中C4流体与甲醇接触 在醚化区(22)中,MTBE向下蒸馏。 然后在氢化区(24)中对未反应的C4进行选择性氢化,其中塔顶残液(108)中的丁二烯减少超过90%。 因此,加氢处理的C4适合于冷酸烷基化或丁二烯有害的其它用途。
    • 8. 发明申请
    • HYDROCONVERSION PROCESS
    • HYDROCONVERSION过程
    • WO1998012281A1
    • 1998-03-26
    • PCT/US1997015128
    • 1997-08-28
    • CHEMICAL RESEARCH & LICENSING COMPANY
    • CHEMICAL RESEARCH & LICENSING COMPANYHICKEY, Thomas, P.HEARN, DennisPUTMAN, Hugh, M.
    • C10G47/02
    • B01D3/009C10G47/00
    • The hydroconversion of heavy petroliferous stocks boiling mainly above 400 DEG F is carried out in a distillation column reactor where concurrently a petroleum stream is fed into a feed zone; hydrogen is fed at a point below said feed zone; the petroleum stream is distilled and contacted in the presence of a cracking catalyst prepared in the form of a catalytic distillation structure at total pressure of less than about 300 psig and a hydrogen partial pressure in the range of 1.0 to less than 70 psia and a temperature in the range of 400 to 1000 DEG F whereby a portion of the petroleum stream is cracked to lighter products boiling below the boiling point of the feed and products are distilled to remove a vaporous overhead stream comprising products mainly boiling below the boiling point of the feed and a liquid bottoms stream.
    • 主要在400°F以上沸腾的重质含油气体的加氢转化在蒸馏塔反应器中进行,同时将石油流进料到进料区; 氢在所述进料区下方的一点进料; 在催化蒸馏结构形式的裂化催化剂存在下蒸馏并接触石油物流,其总压力小于约300psig,氢分压为1.0至小于70psia,温度为 在400至1000°F的范围内,其中一部分石油流被裂解成低于进料沸点沸点的较轻的产物,并蒸馏产物以除去主要沸点低于进料沸点的产物的汽蒸塔顶物流 和液体底部流。
    • 9. 发明申请
    • SELECTIVE HYDROGENATION OF HIGHLY UNSATURATED COMPOUNDS IN HYDROCARBON STREAMS
    • 烃类化合物中高度不饱和化合物的选择性加氢
    • WO1995015934A1
    • 1995-06-15
    • PCT/US1994007758
    • 1994-07-21
    • CHEMICAL RESEARCH & LICENSING COMPANY
    • CHEMICAL RESEARCH & LICENSING COMPANYHEARN, DennisARGANBRIGHT, Robert, P.JONES, Edward, M., Jr.SMITH, Lawrence, A., Jr.GILDERT, Gary, R.
    • C07C05/05
    • C10G70/02C10G45/32
    • A process for the selective hydrogenation of the diolefins and acetylenic compounds in an olefin-rich aliphatic hydrocarbon stream (1) comprises contacting the feed stream (1) at 40-300 DEG F under low hydrogen partial pressure of 0.1-70 psia at a total pressure of 0-350 psig in a distillation column reactor (10) containing a hydrogenation catalyst bed (12) which serves as a component of a distillation structure (10), such as supported PdO encased in a tubular wire mesh. Essentially no hydrogenation of the olefins occur. The feed stream (1) enters below or at the lower end of the catalyst bed (12), and is contacted with hydrogen fed through line (2) in the catalyst bed (12). The overhead (3) is obtained at the overhead, condensed in a condenser (20) and separated in a settler (30), and partially recycled back to catalyst bed (12) as a reflux stream (6). The bottom stream (11) is obtained at the lower end of the distillation reactor, and is partially recycled back as stream (4) after being heated in a heat exchanger (40) as recycle stream (13). Net hydrogenation effluent is obtained as stream (9), and light gases as stream (7).
    • 在富烯烃脂肪族烃流(1)中选择性氢化二烯烃和炔属化合物的方法包括在40-300°F的低氢分压0.1-70psia下将进料流(1)在总共 在含有用作蒸馏结构(10)的成分的氢化催化剂床(12)的蒸馏塔反应器(10)中的压力为0-350psig,例如包裹在管状丝网中的负载PdO。 基本上没有发生烯烃的氢化。 进料流(1)在催化剂床(12)的下端或下端进入,并与在催化剂床(12)中通过管线(2)进料的氢气接触。 塔顶馏出物(3)在顶部获得,在冷凝器(20)中冷凝并在沉降器(30)中分离,并作为回流(6)部分地再循环回催化剂床(12)。 底部物流(11)在蒸馏反应器的下端获得,并且在作为再循环物流(13)的热交换器(40)中加热后,以物流(4)的形式部分地再循环回来。 净氢化流出物作为流(9)获得,轻质气体如流(7)获得。