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公开(公告)号：US4525176A
公开(公告)日：1985-06-25
申请号：US527611
申请日：1983-08-29
Applicant: Wolfgang Koog , Lawrence E. Estabrook
Inventor： Wolfgang Koog , Lawrence E. Estabrook
CPC classification number: B01J19/0026 , C01B3/363 , C10J3/506 , C10J3/526 , C10J3/74 , C10J3/76 , C10J3/78 , C10J3/845 , C10J2300/093 , C10J2300/0943 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0969 , C10J2300/0973 , C10J2300/0976 , C10J2300/1823 , C10J2300/1846 , Y10S48/02
Abstract: The refractory lined reaction zone of a free flow vertical gas generator for the production of raw synthesis gas, reducing gas, or fuel gas by the partial oxidation of an ash-containing solid carbonaceous fuel or a high-metal-containing liquid hydrocarbonaceous fuel is preheated and deslagged by first heating the slag and ash layer on the surface of the refractory lining to a temperature in the range of about 1800.degree.-2000.degree. F. by means of an annular-type elongated burner whose downstream tip is located near the upstream roof of the reaction zone. The tip of the burner is then lowered along the central longitudinal axis of the reaction chamber to above the bottom central outlet passage of the reaction chamber, and the slag and ash layer is heated to their melting point, or above. The molten slag at the bottom of the reaction chamber and the flue gas pass out through the bottom central outlet. The burner is then slowly raised vertically to the initial position while simultaneously melting successive portions of the slag and ash layer on the refractory walls. The molten slag flows down the walls and bottom of the reaction chamber and out through the bottom central outlet passage.
Abstract translation: 用于通过含灰分的固体碳质燃料或含高含金属液体含烃燃料的部分氧化生产原始合成气，还原气体或燃料气体的自由流动垂直气体发生器的耐火衬里反应区被预热 并通过首先将耐火衬里表面上的炉渣和灰分层加热至约1800°-2000°F的温度并通过环形型细长燃烧器将其排渣，该环形细长燃烧器的下游端位于上游屋顶附近 的反应区。 然后将燃烧器的尖端沿着反应室的中心纵向轴线降低到反应室的底部中心出口通道的上方，并将炉渣和灰分层加热到它们的熔点或以上。 反应室底部的熔渣和烟气通过底部中心出口排出。 然后将燃烧器垂直缓慢地升高到初始位置，同时熔化耐火壁上的渣和灰层的连续部分。 熔渣从反应室的壁和底部向下流动，并通过底部中心出口通道流出。
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2.发明授权Process for gas cleaning with reclaimed water and apparatus for water reclamation 失效用回收水进行气体清洗和水回收设备的过程
公开(公告)号：US4205963A
公开(公告)日：1980-06-03
申请号：US955545
申请日：1978-10-27
Applicant: Charles P. Marion , Lawrence E. Estabrook , George N. Richter
Inventor： Charles P. Marion , Lawrence E. Estabrook , George N. Richter
IPC: B01D3/06 , B01D12/00 , C01B3/36 , C01B3/52 , C02F1/04 , C02F1/26 , C10B27/00 , C10J3/46 , C10J3/00 , C01B2/14
CPC classification number: C02F1/048 , B01D12/00 , B01D3/06 , C01B3/36 , C01B3/52 , C02F1/26 , C10J3/485 , C10J3/74 , C10J3/78 , C10J3/84 , C10J3/845 , C10J3/86 , C10K1/101 , C01B2203/0415 , C01B2203/0465 , C01B2203/0475 , C01B2203/048 , C01B2203/0485 , C01B2203/049 , C01B2203/0495 , C10J2300/093 , C10J2300/0943 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0976 , C10J2300/1807 , C10J2300/1846 , C10J2300/1884 , C10J2300/1892
Abstract: Dispersions comprising water and particulate solids i.e. carbon and ash are produced in at least one gas cooling or scrubbing zone by quench cooling or scrubbing the raw gas stream from a partial oxidation gas generator with water. The dispersions are resolved by liquid extraction in a decanting zone to produce a water layer containing carbon, dissolved gas, and ash, and also a separate dispersion comprising carbon, extractant, and water. Solids-free water, liquid extractant and uncondensed gases are then separated from each other in a distillation and separation operation. Water is removed from a separation vessel in said operation and introduced on to a stripping plate of a flash column containing at least one stripping plate. The solids-containing water from the decanting zone is flashed below said stripping plate and a portion is converted into steam. The steam passes up through holes or bubble caps in the stripping plate and is dispersed through the water contained on said plate. If desired, a portion of the water obtained from blowing-down a gas cooler may be flashed to steam below the stripping plate. Unvaporized water falls to the bottom of the column where a vertical weir separates the flash column into two chambers. Solids settle out of the water in the first chamber and clarified water flows over the weir into the second chamber. Overflow water from the bottom stripping plate is discharged below the water-level in the second chamber by way of a downcomer. Reclaimed water is pumped to said gas cooling and scrubbing zones from the second chamber, and waste water containing solids in the first chamber is discharged from the system. The overhead from the flash column is cooled below the dew point and introduced into said separation vessel.
Abstract translation: 包含水和颗粒固体（即碳和灰分）的分散体在至少一个气体冷却或洗涤区中通过淬火冷却或用水洗涤来自部分氧化气体发生器的原料气流而产生。 通过在倾析区域中的液体萃取来分离分散体，以产生含有碳，溶解气体和灰分的水层，以及包含碳，萃取剂和水的单独分散体。 然后在蒸馏和分离操作中将无固体水，液体萃取剂和未冷凝的气体彼此分离。 在所述操作中从分离容器中除去水，并将其引入到含有至少一个剥离板的闪蒸塔的剥离板上。 来自倾析区域的含固体的水在所述剥离板下方闪蒸，并将一部分转化为蒸汽。 蒸汽通过汽提板中的孔或气泡盖，并通过包含在所述板上的水分散。 如果需要，从吹气气体冷却器获得的一部分水可以被闪蒸到汽提板下方的蒸汽。 未蒸发的水落到塔的底部，垂直的堰将闪蒸塔分成两个室。 固体沉积在第一个室中的水中，澄清的水流过堰进入第二个室。 来自底部剥离板的溢流水通过降液管排放到第二室中的水位以下。 回收水被泵送到来自第二室的所述气体冷却和洗涤区域，并且在第一室中含有固体的废水从系统中排出。 将闪蒸塔的塔顶馏出物冷却至低于露点并引入所述分离容器中。
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公开(公告)号：US4490251A
公开(公告)日：1984-12-25
申请号：US460411
申请日：1983-01-24
Applicant: Manuel E. Quintana , Lawrence E. Estabrook
Inventor： Manuel E. Quintana , Lawrence E. Estabrook
Abstract: A novel vertical decanter is provided comprising a vertical cylindrical vessel with separate inner and outer coaxial concentric conduits that pass down through the central axial flanged inlet in the upper head of the vessel. The mixture of soot-water dispersion and first liquid organic extractant i.e. naphtha is passed through the inner conduit and is discharged through a first horizontal radial nozzle located below the interface level. Simultaneously, the second liquid organic extractant i.e. liquid organic by-products from an oxo or oxyl process is passed through the annular passage between the inner and outer conduits and is discharged through a second horizontal radial nozzle located above the interface level. Adjusting means are provided to vary the discharge height of the second horizontal radial nozzle, up or down should there be a change in location of the interface level.
Abstract translation: 提供了一种新颖的垂直倾析器，其包括具有分离的内部和外部同轴同心导管的垂直圆柱形容器，其向下穿过容器的上部头部中的中心轴向凸缘入口。 烟灰水分散体和第一液体有机萃取剂（即石脑油）的混合物通过内部导管，并通过位于界面水平以下的第一水平径向喷嘴排出。 同时，第二液体有机萃取剂即来自氧代或氧化方法的液体有机副产物通过内导管和外管之间的环形通道，并通过位于界面水平以上的第二水平径向喷嘴排出。 提供调整装置，以便在界面水平位置发生变化时，上下移动第二水平径向喷嘴的排放高度。
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公开(公告)号：US4385906A
公开(公告)日：1983-05-31
申请号：US352443
申请日：1982-02-25
Applicant: Lawrence E. Estabrook
Inventor： Lawrence E. Estabrook
CPC classification number: C01B3/36 , C10J3/466 , C10J3/526 , C10J3/726 , C10J3/74 , C10J3/78 , C10J3/84 , C10J2300/093 , C10J2300/0943 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0976 , C10J2300/1807 , C10J2300/1823 , C10J2300/1846
Abstract: A method for starting up a pressurized partial oxidation gas generation system comprising a gas generator and gas purification train without atmospheric pollution. The method comprises isolating and prepressuring the gas purification train to a pressure of at least 50 percent of normal operating pressure, starting the gas generator and autogenously increasing the pressure in the gas generator to the pressure of the gas purification train before establishing communication with the gas purification train to permit flow of gas through the gas purification train. Purified gases discharged from the gas purification train may be burned in a flare without atmospheric pollution.
Abstract translation: 一种用于启动加压部分氧化气体发生系统的方法，包括气体发生器和气体净化系统，而无大气污染。 该方法包括将气体净化系统分离和预压至正常工作压力的至少50％的压力，启动气体发生器并在与气体建立通信之前自动增加气体发生器中的压力至气体净化系统的压力 净化列车允许气体通过气体净化列车。 从气体净化系统排出的净化气体可能在没有大气污染的火炬中燃烧。
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5.发明授权Process for gas cleaning with reclaimed water and apparatus for water reclamation 失效用回收水进行气体清洗和水回收设备的过程
公开(公告)号：US4141696A
公开(公告)日：1979-02-27
申请号：US900951
申请日：1978-04-28
Applicant: Charles P. Marion , Lawrence E. Estabrook , George N. Richter
Inventor： Charles P. Marion , Lawrence E. Estabrook , George N. Richter
IPC: B01D3/06 , B01D12/00 , C01B3/36 , C01B3/52 , C02F1/04 , C02F1/26 , C10B27/00 , C10J3/46 , C10J3/00 , C01B2/14
CPC classification number: C01B3/52 , B01D12/00 , B01D3/06 , C01B3/36 , C02F1/048 , C02F1/26 , C10J3/485 , C10J3/74 , C10J3/78 , C10J3/84 , C10J3/845 , C10J3/86 , C10K1/101 , C10K3/04 , C01B2203/0415 , C01B2203/0465 , C01B2203/0475 , C01B2203/048 , C01B2203/0485 , C01B2203/049 , C01B2203/0495 , C10J2300/093 , C10J2300/0943 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0976 , C10J2300/1675 , C10J2300/1807 , C10J2300/1846 , C10J2300/1884 , C10J2300/1892
Abstract: Dispersions comprising water and particulate solids i.e. carbon and ash are produced in at least one gas cooling or scrubbing zone by quench cooling or scrubbing the raw gas stream from a partial oxidation gas generator with water. The dispersions are resolved by liquid extraction in a decanting zone to produce a water layer containing carbon, dissolved gas, and ash, and also a separate dispersion comprising carbon, extractant, and water. Solids-free water and liquid extractant are then separated from said dispersion in a distillation zone. This water is introduced on to a stripping plate of a flash column along with solids-free recycle condensate from the flash column. The solids-containing water from the decanting zone is flashed below said stripping plate and a portion is converted into steam. The steam passes up through holes or bubble caps in the stripping plate and is dispersed through the water contained on said plate. If desired, a portion of the water obtained from blowing-down a gas cooler may be flashed to steam below the stripping plate. Unvaporized water falls to the bottom of the column. A vertical weir separates the flash column at the bottom into two chambers. Solids settle out of the water in the first chamber and clarified water flows over the weir into the second chamber. Overflow water from the stripping plate is discharged below the water-level in the second chamber by way of a downcomer. Reclaimed water is pumped to said gas cooling and scrubbing zones from the second chamber, and waste water containing solids in the first chamber is discharged from the system.
Abstract translation: 包含水和颗粒固体（即碳和灰分）的分散体在至少一个气体冷却或洗涤区中通过淬火冷却或用水洗涤来自部分氧化气体发生器的原料气流而产生。 通过在倾析区域中的液体萃取来分离分散体，以产生含有碳，溶解气体和灰分的水层，以及包含碳，萃取剂和水的单独分散体。 然后将无固体水和液体萃取剂与蒸馏区中的所述分散体分离。 将该水引入闪蒸塔的剥离板以及来自闪蒸塔的无固体循环冷凝物。 来自倾析区域的含固体的水在所述剥离板下方闪蒸，并将一部分转化为蒸汽。 蒸汽通过汽提板中的孔或气泡盖，并通过包含在所述板上的水分散。 如果需要，从吹气气体冷却器获得的一部分水可以被闪蒸到汽提板下方的蒸汽。 未蒸发的水落在塔底部。 垂直堰将底部的闪蒸塔分成两个室。 固体沉积在第一个室中的水中，澄清的水流过堰进入第二个室。 来自剥离板的溢流水通过降液管排放到第二室中的水位以下。 回收水被泵送到来自第二室的所述气体冷却和洗涤区域，并且在第一室中含有固体的废水从系统中排出。
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Patent Agency Ranking
公开(公告)号：US4466810A
公开(公告)日：1984-08-21
申请号：US445388
申请日：1982-11-29
Applicant: Roger M. Dille , George N. Richter , Lawrence E. Estabrook , Jean-Georges P. Rohner , Harold A. Rhodes
Inventor： Roger M. Dille , George N. Richter , Lawrence E. Estabrook , Jean-Georges P. Rohner , Harold A. Rhodes
CPC classification number: C10J3/485 , C10J3/526 , C10J3/74 , C10J3/78 , C10J3/84 , C10J3/845 , C10K1/101 , C10J2300/093 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0976 , C10J2300/1671 , C10J2300/169 , C10J2300/1807 , C10J2300/1884 , C10J2300/1892
Abstract: A continuous process for preventing the build-up of metals from the hydrocarbonaceous fuel feed in a partial oxidation system in which about 80-100 wt. % of the carbon-soot produced is recycled to the gas generator. By the subject process a significantly large portion of the metals and metal compounds i.e. ash in the soot-water feed stream to the decanter become concentrated in the grey water that separates out in the decanter in the carbon recovery section. The concentration of ash suspended in the grey water may be then easily reduced in a solids-liquid separator with or without the addition of a flocculant and prior to recycling a portion of the grey water to the gas quench tank and/or gas scrubber. Further, the ash suspended in the carbon-soot-liquid hydrocarbonaceous fuel stream from the bottom of the liquid organic extractant still may be optionally reduced in another solids-liquid separator prior to recycling a portion of said stream to the gas generator as part of the hydrocarbonaceous reactant fuel feed.
Abstract translation: 一种连续的方法，用于防止在部分氧化体系中来自含烃燃料进料的金属的累积，其中约80-100wt。 产生的碳烟的％被再循环到气体发生器。 通过本发明方法，大量的金属和金属化合物，即向倾析器的烟灰 - 水进料流中的灰分变得集中在在碳回收部分的滗析器中分离的灰水中。 在有或没有添加絮凝剂的情况下，并且在将一部分灰水再循环到气体骤冷罐和/或气体洗涤器之前，可以在固体 - 液体分离器中容易地减少悬浮在灰水中的灰分浓度。 此外，从液体有机萃取剂底部悬浮在碳烟煤 - 液体烃类燃料物流中的灰分，在将一部分所述物流再循环到气体发生器之前，还可以任选地在另一固体 - 液体分离器中还原，作为 含烃反应物燃料进料。
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公开(公告)号：US4436531A
公开(公告)日：1984-03-13
申请号：US412437
申请日：1982-08-27
Applicant: Lawrence E. Estabrook , Robert M. Suggitt
Inventor： Lawrence E. Estabrook , Robert M. Suggitt
IPC: C10J3/46
CPC classification number: C10J3/466 , C10J3/526 , C10J3/74 , C10J3/84 , C10K1/046 , C10K1/06 , C10K1/103 , C10K1/122 , C10K3/023 , C10J2300/093 , C10J2300/0943 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0973 , C10J2300/0976 , C10J2300/0996 , C10J2300/1823 , C10J2300/1846 , C10J2300/1884 , C10J2300/1892 , Y10S48/07
Abstract: Synthesis gas, fuel gas, or reducing gas is produced by the noncatalytic partial oxidation of a slurry of ash-containing solid carbonaceous fuel in a liquid carrier with a free-oxygen containing gas in the free-flow reaction zone of a refractory lined gas generator at an autogenous temperature in the range of about 2350.degree. F. to 2900.degree. F. so that about 75 to 95 weight percent of the carbon in the fuel feed to the reaction zone is converted into carbon oxides. The hot effluent gas stream from the reaction zone containing entrained particulate carbon, unconverted solid carbonaceous fuel, and molten slag is passed through a free-flow radiant cooler where it is contacted by and provides the heat to vaporize an aqueous solution of catalyst consisting of alkali metal and/or alkaline earth metal compound in water. In the presence of the catalyst, H.sub.2 O and at least a portion of the particulate carbon and the carbon in the unconverted solid carbonaceous fuel are reacted together at a controlled temperature to produce additional H.sub.2 and CO.sub.x. The hot effluent gas stream enters the radiant cooler at a temperature in the range of about 2800.degree. F.-2300.degree. F. and leaves at a temperature in the range of about 1350.degree. F.-1600.degree. F. Further, the molten slag in the effluent gas stream may be fluxed with the alkali metal and/or alkaline earth metal compound to facilitate separation of the slag from the effluent gas stream.
Abstract translation: 合成气体，燃料气体或还原气体是通过在耐火衬里气体发生器的自由流动反应区中的具有含游离氧气体的液体载体中的含灰分固体碳质燃料的浆料的非催化部分氧化产生的 在约2350°F至2900°F范围内的自生温度下，使得进入反应区域的燃料中约75至95wt％的碳转化为碳氧化物。 来自含有夹带的颗粒碳，未转化的固体碳质燃料和熔渣的反应区的热废气流通过自由流辐射冷却器，在其中与其接触并提供热量以蒸发由碱组成的催化剂水溶液 金属和/或碱土金属化合物在水中。 在催化剂的存在下，H 2 O和未转化的固体碳质燃料中的至少一部分颗粒碳和碳在受控的温度下一起反应以产生额外的H 2和CO x。 热废气流在约2800°F-2300°F的温度范围内进入辐射冷却器，并在约1350°F-1600°F范围内离开。此外，熔渣 在废气流中可以用碱金属和/或碱土金属化合物进行助熔，以便于从流出气流中分离炉渣。
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公开(公告)号：US4411817A
公开(公告)日：1983-10-25
申请号：US301348
申请日：1981-09-11
Applicant: James F. Elliott , George N. Richter , Lawrence E. Estabrook
Inventor： James F. Elliott , George N. Richter , Lawrence E. Estabrook
IPC: C10J3/46
CPC classification number: C10J3/46 , C10J3/52 , C10J3/526 , C10J3/78 , C10J3/84 , C10J2300/093 , C10J2300/0943 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0973 , C10J2300/0976 , C10J2300/1846 , C10J2300/1884
Abstract: In a high pressure process for the production of synthesis gas from ash-containing fuels where the ash is collected in water in a settling zone below the gasification chamber, bridging by the slag in the narrower sections of the settling zone is avoided by passing a gas upwardly through the settling zone water.
Abstract translation: 在用于从含有灰分的燃料生产合成气的高压法中，其中灰分在气化室下方的沉降区中被收集在水中，通过使气体通过气体的较窄部分中的炉渣而桥接 向上通过沉降区水。
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公开(公告)号：US4205962A
公开(公告)日：1980-06-03
申请号：US955544
申请日：1978-10-27
Applicant: Charles P. Marion , Lawrence E. Estabrook , George N. Richter
Inventor： Charles P. Marion , Lawrence E. Estabrook , George N. Richter
IPC: B01D3/06 , B01D12/00 , C01B3/36 , C01B3/52 , C02F1/04 , C02F1/26 , C10B27/00 , C10J3/46 , C10J3/00 , C01B2/14
CPC classification number: C10J3/485 , B01D12/00 , B01D3/06 , C01B3/36 , C01B3/52 , C02F1/048 , C02F1/26 , C10J3/74 , C10J3/78 , C10J3/84 , C10J3/845 , C10J3/86 , C10K1/101 , C01B2203/0415 , C01B2203/0465 , C01B2203/0475 , C01B2203/048 , C01B2203/0485 , C01B2203/049 , C01B2203/0495 , C10J2300/093 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/0976 , C10J2300/1807 , C10J2300/1846 , C10J2300/1884 , C10J2300/1892
Abstract: Dispersions comprising water and particulate solids i.e. carbon and ash are produced in at least one gas cooling or scrubbing zone by quench cooling or scrubbing, or both the raw gas stream from a partial oxidation gas generator with water. Advantageously, the water may be reclaimed by the subject process. In one embodiment, the carbon-water dispersion containing any ash is mixed with a liquid organic extractant and a liquid aqueous emulsion. The emulsion breaks up, and in a decanting operation a carbon-extractant-water dispersion containing gaseous impurities separates out and floats on a dilute bottoms water layer containing gaseous impurities and some solids. The carbon-extractant-water dispersion is mixed with a heavy liquid hydrocarbon and introduced into a distillation column. The overhead from the distillation column is cooled and separated in a separation vessel into an upper layer of liquid organic extractant, an intermediate layer of aqueous emulsion, a bottom layer of water, and an overhead stream of uncondensed gaseous impurities if any. The liquid aqueous emulsion and the liquid extractant are recycled to the decanting operation. The water layer from the separation vessel and the bottoms water from the decanting operation are separately introduced into a flash column where the water is reclaimed. The flash column includes at least one stripping plate and two chambers at the bottom separated by a weir. The overhead from the flash column is cooled below the dew point and is introduced into said separation vessel. In another scheme, the emulsion is mixed with the bottoms water from the decanting operation and fed to a flash column for reclaiming water. Alternately, the aqueous emulsion is broken-up into water and liquid hydrocarbon by heating.
Abstract translation: 包含水和颗粒固体（即碳和灰分）的分散体通过淬火冷却或洗涤或者来自部分氧化气体发生器的原料气体流与水在至少一个气体冷却或洗涤区中产生。 有利地，水可以通过主题过程回收。 在一个实施方案中，含有任何灰分的碳水分散体与液体有机萃取剂和液体水性乳液混合。 乳液分解，并且在倾析操作中，含有气态杂质的碳萃取剂 - 水分散体分离出来，漂浮在含有气态杂质和一些固体的稀的底部水层上。 将碳萃取剂 - 水分散体与重质液体烃混合并引入蒸馏塔。 来自蒸馏塔的塔顶馏出物在分离容器中被冷却并分离成液体有机萃取剂的上层，水性乳液的中间层，底部的水，以及未冷凝的气态杂质的顶部物流（如果有的话）。 将液体水性乳液和液体萃取剂再循环至倾析操作。 来自分离容器的水层和来自倾析操作的底部水分别引入闪蒸塔中，其中回收水。 闪蒸塔包括至少一个剥离板和在底部由堰隔开的两个室。 将闪蒸塔的塔顶馏出物冷却至低于露点并引入所述分离容器中。 在另一种方案中，将乳液与来自倾析操作的底部水混合，并送入闪蒸塔以回收水。 或者，水乳液通过加热分解成水和液体烃。
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公开(公告)号：US4007017A
公开(公告)日：1977-02-08
申请号：US643069
申请日：1975-12-22
Applicant: William L. Slater , George N. Richter , William B. Crouch , Lawrence E. Estabrook
Inventor： William L. Slater , George N. Richter , William B. Crouch , Lawrence E. Estabrook
CPC classification number: C01B3/50 , C01B3/36 , C10J3/485 , C10J3/74 , C10J3/78 , C10J3/84 , C10K1/04 , C10K1/10 , C01B2203/049 , C10J2300/093 , C10J2300/0943 , C10J2300/0946 , C10J2300/0956 , C10J2300/0959 , C10J2300/1675 , C10J2300/1807 , C10J2300/1846 , C10J2300/1884 , C10J2300/1892
Abstract: An improved continuous partial oxidation process for producing clean synthesis or fuel gas from a hydrocarbonaceous fuel feed is disclosed wherein the effluent gas stream from the reaction zone of the gas generator is simultaneously cooled and cleaned by first discharging the gas stream directly into a relatively large body of hot liquid hydrocarbon immersion fluid contained in an immersion vessel, and second by scrubbing with by-product water obtained subsequently in the process in a nozzle scrubber. The process gas stream is optionally cooled and passed into a gas-liquid separator where any condensed by-product noxious water and any C.sub.5 -C.sub.10 liquid hydrocarbons are separated from each other and from the clean product gas stream. By-product noxious water is disposed of without polluting the environment by recycling a portion of it to the gas generator as the temperature moderator. For example, the immersion fluid may be a dispersion of liquid hydrocarbonaceous fuel such as petroleum oil and particulate carbon which is contained in a separate immersion vessel. A portion of the hot immersion fluid is continuously removed from the immersion vessel and is cooled in an external gas cooler to a temperature in the range of about 300.degree. to 850.degree. F but above the dew point of the water in the process gas stream. Portions of the cooled immersion fluid are recycled to the immersion vessel, and optionally to the gas generator as at least a portion of the hydrocarbonaceous fuel feed. In another embodiment, a portion of the immersion fluid removed from the immersion vessel may be introduced into the gas generator as at least a portion of the feed without first being passed through a cooler. The clean product gas comprises H.sub.2, CO, CO.sub.2, H.sub.2 O and, optionally at least one material from the group H.sub.2 S, COS, N.sub.2, A, and C.sub.1 -C.sub.4 hydrocarbons.
Abstract translation: 公开了一种用于从烃类燃料进料中产生清洁合成或燃料气体的改进的连续部分氧化方法，其中来自气体发生器的反应区的流出气体流同时被冷却和清洁，首先将气流直接排放到相对大的体内 包含在浸没容器中的热液体烃浸液，其次通过在喷嘴洗涤器中随后在该方法中获得的副产物水进行洗涤。 任选地将工艺气流冷却并进入气液分离器，其中任何冷凝的副产物有害水和任何C5-C10液体烃彼此分离，并且与清洁产物气流分离。 通过将副产物的一部分再循环到作为温度调节剂的气体发生器中，副产物有害水被处理而不污染环境。 例如，浸渍流体可以是液体烃类燃料如石油和分散在容器中的颗粒状碳的分散体。 热浸液体的一部分从浸没容器中连续地取出，并在外部气体冷却器中冷却至约300-850°F，但高于工艺气体流中的水的露点。 冷却的浸没流体的一部分被再循环到浸没容器中，并且任选地再循环到作为含烃燃料进料的至少一部分的气体发生器。 在另一个实施例中，从浸没容器移除的浸渍流体的一部分可以作为进料的至少一部分被引入到气体发生器中，而不首先通过冷却器。 清洁产品气体包括H 2，CO，CO 2，H 2 O和任选的至少一种来自H 2 S，COS，N 2，A和C 1 -C 4烃的材料。
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