Abstract: An ash filter and reboiler (ash filter/reboiler) includes an inlet tube heat exchanger including an outer column (column) having a vapor inlet tube through an inlet of the column coupled therein to receive fuel vapors including entrained ash particles and to direct the fuel vapors including the entrained ash particles out from a bottom of the vapor inlet tube toward a bottom portion of the column. A cooler over the bottom portion of the column for condensing the fuel vapors including the entrained ash particles to liquid fuel. A pump coupled to an outlet in a bottom of the column is for pumping out an ash particle laden portion of the liquid fuel. A heater is above the cooler for vaporizing the liquid fuel into reboiled vapor, and a vapor outlet is at a top of the column for releasing the reboiled vapors out from the column.

Abstract: A reactor allowing continuous regeneration of catalyst grains having a chamber with an oxychlorination zone superposed on a calcination zone equipped with a pipe for introducing calcination gas and at least one pipe for injecting oxychlorination gas emptying into the inner space. Each gas passage has a gas evacuation device that is permeable to gas and impermeable to catalyst grains.

Abstract: A multi-effects desalination system includes a housing having a heating box, a plurality of vessels, a plurality of heat rods within each of the vessels, and a condenser unit. Each vessel is separated by a separator wall. Each heat rod extends through one of the separator walls, such that each heat rod has a first end extending into one vessel and a second end extending into an adjacent vessel. The desalination system also includes a plurality of sprayers, a plurality of demisters, and a plurality of trays. Each sprayer is configured to discharge feed water FW onto the second end of each heat rod in a respective vessel and each tray being configured to collect condensate or fresh water. The condensate collected in one to tray can be transferred to the condensate collection tray in an adjacent vessel. Further, the desalination system can also include a thermocompressor unit.

Abstract: Disclosed herein is a process for catalytically reforming naphtha, comprising, in the presence of hydrogen gas, contacting naphtha with at least one reforming catalyst under the conditions of a pressure ranging from 0.15 to 3.0 MPa, a temperature ranging from 300 to 540° C., a volume space velocity ranging from 2.1 to 50 h?1, to carry out a shallow catalytic reforming reaction so as to achieve a naphthene conversion ratio of greater than 85 mass %, and a conversion ratio of paraffins to arenes and C4? hydrocarbons of less than 30 mass %.

Abstract: An apparatus for the discharge of quenched or unquenched coke from a coke quenching car into a receiving device, providing that there is an extension of the pusher machine beside at least one coke-oven chamber, which is arranged in one line with the coke-oven chambers, and which is to be operated by the pusher machine, and that there is a receiving device behind the quenching car as seen from the coke-oven battery into which the coke can be pushed from the quenching car by the extension, the receiving device preferably being a wharf. A process for the discharge of the hot coke from a coke quenching car into a receiving device is also disclosed. Capacity bottlenecks of the quenching equipment are compensated so that the coke need not stay in the coke-oven chamber after the end of the coking process, or disturbances of the quenching equipment can be compensated temporarily.

Abstract: Disclosed is a method for selectively separating and recovering silicon from waste silicon sludge generated during a semiconductor manufacturing process. With the method for separating and recovering silicon from the silicon sludge, oil components, iron, silicon carbide that are included in the silicon sludge may be removed and silicon may be selectively separated and recovered. In addition, silicon may be efficiently recovered without injection of an additive for precipitating a specific component or without a separate device such as a magnetic separator, or the like, for removing iron.

Abstract: A reactor for regenerating catalyst grains comprises a vessel having an oxychlorination zone superimposed over a calcining zone having a line for introducing gas. A chamber, disposed between oxychlorination and calcining zones, comprises an internal space located between two plates which are gas tight and impervious to catalyst grains. A plurality of tubes pass through the chamber to allow catalyst to pass from oxychlorination zone to calcining zone. A plurality of means pass through the chamber to allow calcining gas to pass from calcining zone to oxychlorination zone. At least one oxychlorination gas injection line opens into the internal space of the chamber. Each means for passage of calcining gas comprises at least one orifice communicating with the chamber internal space, and a means for evacuating gas which is permeable to gas and impermeable to catalyst grains.

Abstract: A method and system are disclosed for co-production of olefins and electric power. The method includes determining a separation level, separating a hydrocarbon feed into a light fraction stream and a heavy fraction stream based on the determined separation level; generating electric power from the heavy fraction stream; and cracking the light fraction stream in a pyrolysis unit to produce an effluent comprising olefins. The separation level may be based on olefin production requirements and electric power requirements or specific split of the hydrocarbon feed to be utilized for power generation and olefin production.

Abstract: A process is provided that is directed to a steam pyrolysis zone integrated with a hydroprocessing zone including residual bypass to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics.

Abstract: Deep desulfurization of hydrocarbon feeds containing undesired organosulfur compounds to produce a hydrocarbon product having low levels of sulfur, i.e., 15 ppmw or less of sulfur, is achieved by flashing the feed at a target cut point temperature to obtain two fractions. A first fraction contains refractory organosulfur compounds, which boil at or above the target cut point temperature. A second fraction boiling below the target cut point temperature is substantially free of refractory sulfur-containing compounds. The second fraction is contacted with a hydrodesulfurization catalyst in a hydrodesulfurization reaction zone operating under mild conditions to reduce the quantity of organosulfur compounds to an ultra-low level. The first fraction is contacted with an oxidizing agent and an active metal catalyst in an oxidation reaction zone to convert the refractory organosulfur compounds to oxidized organosulfur compounds.

Abstract: A process is provided that is directed to a steam pyrolysis zone integrated with a solvent deasphalting zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated solvent deasphalting and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises charging the crude oil to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase; thermally cracking the deasphalted and demetalized oil stream in the presence of steam to produce a mixed product stream; separating the mixed product stream; recovering olefins and aromatics from the separated mixed product stream; and recovering pyrolysis fuel oil from the separated mixed product stream.

Abstract: A process is provided that is directed to a steam pyrolysis zone integrated with a solvent deasphalting zone and a hydrotreating zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics.

Abstract: Steam pyrolysis and hydroprocessing are integrated including hydrogen redistribution to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. A feed is initially split into a light portion and a heavy portion, and the heavy portion is hydroprocessed. A hydroprocessed effluent is charged, along with steam, to a convection section of a steam pyrolysis zone. The mixture is heated and passed to a vapor-liquid separation section. A residual portion is removed and light components are charged to a pyrolysis section of the steam pyrolysis zone. A mixed product stream is recovered from the steam pyrolysis zone and it is separated into product including olefins and aromatics.

Abstract: The invention relates to a method for reducing nitrogen oxides from the exhaust gas of a coke oven, which has a plurality of coking chambers and heating walls, arranged between the coking chambers, with heating flues (12, 12?) for the indirect heating of the coking chambers. A combustible gas (16), which consists entirely or partially of coke oven gas, is burned in the heating flues (12, 12?), thereby producing an exhaust gas which contains nitrogen oxides. A reducing agent is fed to the exhaust gas at a temperature between 700° C. and 1100° C. and the proportion of nitrogen oxide in the exhaust gas is reduced by a homogeneous gas reaction between the reducing agent and the nitrogen oxides. The exhaust gas is subsequently passed through a regenerator (4) for heat recovery.

Abstract: Described herein is an oil extraction device comprising a housing; a first trough resting within an upper portion of said housing, where said first trough holds a solvent; a heat source within said housing, where said heat source heats said first trough; a control device mounted within said housing, where said control device controls said heat source; a reservoir attached to said upper portion of said housing; a strainer basket positioned within said reservoir, where said strainer basket holds an extraction substance; a filter fitted within said strainer basket below said extraction substance; a second filter positioned above said extraction substance; a condenser positioned above said housing; a second trough positioned at a bottom portion of said condenser; and a set of flanges extruding from said condenser, where said set of flanges enable said condenser to cool and condense solvent vapor when operating said oil extraction device.

Abstract: A mixture containing methyldichlorosilane, tetrachlorosilane, and trichlorosilane is distilled to fractionate a fraction with a higher content of methyldichlorosilane than the mixture before distillation. Subsequently, the fraction thus fractionated is heated to disproportionate chlorine between methyldichlorosilane and tetrachlorosilane to disproportionate methyldichlorosilane into methyltrichlorosilane. Subsequently, the fraction after disproportionation containing methyltrichlorosilane is purified by distillation to separate high-purity trichlorosilane. Having a close boiling point to that of trichlorosilane (32° C.), which is a target product to be purified by distillation, removal of methyldichlorosilane (boiling point of 41° C.) has been difficult. The present invention removes methyldichlorosilane more easily by converting it into methyltrichlorosilane (boiling point of 66° C.) through disproportionation of chlorine between methyldichlorosilane and tetrachlorosilane.

Abstract: The invention is directed towards a method of removing mercury bearing species from a hydrocarbon containing fluid. The method comprises the steps of: i) adding dithiocarbamate polymer to the fluid in an amount such that the number of mercury bonding sites on the polymer exceeds the amount of mercury atoms by at least 10% and ii) removing the mercury bearing dithiocarbamate polymer with a water/oil separation device. The invention relies upon an unexpected reversal in the solubility of dithiocarbamate polymer at very high concentrations. Because of the high solubility the polymer remains within the water phase of the hydrocarbon fluid and can be removed without the need for cumbersome precipitation methods and complicated solid liquid separation devices.

Abstract: A multistage thermal desalination system, together with its associated method of use, allows de-scaling of subsystems exposed to saturated saltwater by alternating the saturation stage of the process between two neighboring physical desalination stages. The desalination system is provided with at least one transfer conduit, at least one pump, and valving to permit saltwaters being desalinated by higher and lower stage desalination subsystems to be swapped. By replacing the saturated saltwater in a higher salt concentration desalination subsystem with lower salt concentration saltwater, the scaling in higher salt concentration desalination subsystem is reduced while the saturation load is placed on another of the desalination subsystems.

Abstract: A thermal distillation system comprises heating means and cooling means arranged to heat and cool, respectively, treatable liquid in a liquid circuit having a first section between a heating means output and cooling means input, and a second section between an a cooling means output and heating means input, and further comprises distillation stages, each including an evaporator on the first section and a condenser on the second section in heat exchange relationship with liquid in the second section, a carrier gas circuit, on which the evaporator and condenser are arranged, and an output for outputting liquid extracted, wherein the stages are arranged such that their evaporators are disposed along the first section in a direction from the heating means to the cooling means and their condensers are disposed in corresponding order along the second section in a direction from the heating means to the cooling means.

Abstract: The present invention provides a process for deep desulphurization of cracked gasoline with minimum octane loss of about 1-2 units. In this process full range cracked gasoline from FCC, Coker, Visbreaker etc is sent to Diolefin Saturation Reactor for selective saturation of diolefins. After saturation of diolefins, the stream is sent to Splitter for splitting into three cuts i.e Light Cut (IBP-70° C.), Intermediate Cut (70-90° C.) and Heavy Cut (90-210° C.). The Light Cut which contains majority of the high octane olefins and mercaptan sulfur is desulfurized with caustic treatment using Continuous Film Contactor (CFC). The sulfur in the Intermediate Cut is also predominantly mercaptans and the cut can be desulfurized by caustic treatment using CFC along with Light cut or separately desulfurized before being sent for isomerization. The Heavy Cut containing mainly thiophinic sulfur compounds is treated either by using conventional HDS process or reactive adsorption process.