The invention generally relate to processes, systems, and methods for the pyrolysis of hydrocarbon feeds containing one or more forms of mercury, e.g., the steam cracking of heavy oil, such as crude oil. Effluent from the pyrolysis is processed to remove various forms of mercury produced during the pyrolysis and/or carried over from the hydrocarbon feed.

A method for recovering C2 components in a methane-containing industrial gas includes the steps of (1) cooling a compressed methane-containing industrial gas and performing gas-liquid separation; (2) absorbing C2 components in the gas phase by using an absorbent to obtain an absorption rich liquid; (3) returning the absorption rich liquid to the compression in step (1) or mixing the absorption rich liquid with the liquid phase obtained in step (1) to obtain a mixed liquid, and depressurizing the mixed liquid or the absorption rich liquid; (4) performing methane desorption on the depressurized stream to obtain a rich absorbent, or performing second gas-liquid separation on the depressurized stream, followed by methane desorption on the second liquid phase to obtain a rich absorbent; and (5) desorbing and separating the rich absorbent to obtain a lean absorbent and an enriched gas, and recycling and reusing the lean absorbent.

A method for the desulfurization and separation of a catalytic cracking light product includes the steps of: 1) contacting a catalytic cracking light product with a desulfurization adsorbent in an adsorption desulfurization reaction unit in the presence of hydrogen for desulfurization, and optionally, carrying out gas-liquid separation on the resulting desulfurization product, to obtain a desulfurized rich gas and a desulfurized crude gasoline, wherein the catalytic cracking light product is an overhead oil-gas fraction from a catalytic cracking fractionator, or a rich gas and a crude gasoline from a catalytic cracking fractionator; and 2) separately sending the desulfurized rich gas and the desulfurized crude gasoline obtained in the step 1) to a catalytic cracking absorption stabilization system for separation, to obtain a desulfurized dry gas, a desulfurized liquefied gas and a desulfurized stabilized gasoline.

The present invention relates to an apparatus that is part of a reusable fuel processing unit that allows the absorption of char contained within vapor that is leaving the reactor including a gear box, gearbox housing, support flange and seal, exhaust housing, exhaust port, connecting flange, screw top split housing, vertical steal housing, three augers with drive shafts on each auger contained within the steel housing, discharge flange, support ring, expansion cart, and cam followers.

The present subject matter relates generally to methods for selectively saturating the unsaturated C.sub.2-C.sub.4. More specifically, the present subject matter relates to methods for saturating butadiene and butenes from a hydrocarbon stream before it is combined with a fresh feed and enters a reaction zone. Removing the unsaturates from the hydrocarbon stream before the hydrocarbon stream enters the reaction zone prevents the reactor internals from coking.

The invention relates to mixtures comprising molecular hydrogen, hydrocarbons, and nitrogen oxides; to processes for removing at least a portion of the nitrogen oxides therefrom; to equipment useful in such processes; and to the use of such hydrocarbons for, e.g., chemical manufacturing.

In an FCC apparatus and process structured packing should be located at the very top of the stripping section in an upper region. The lower region below the structural packing may be equipped with fluidization equipment such as stripping media distributors and one or more gratings. This arrangement enables stripping of entrained hydrocarbons off the incoming catalyst immediately upon entry into the stripping section allowing the entrained hydrocarbon to exit the stripping section with minimized residence time to minimize post-riser cracking. Revamp of stripping sections with tall stripping sections should conducted in this way to improve performance and reduce down-time for equipment installation.

The preset invention provides an energy-saving process and device for recovering C2 from refinery dry gas. The process is as follows: dry gas is cooled and then sent to a multi-stage absorption tower for treatment; the gas phase from the multi-stage absorption tower is sent to a fuel gas pipeline network or PSA unit, and the liquid phase is sent to a high-pressure flash zone for treatment; the gas phase from the high-pressure flash zone is returned to a compression section of a dry gas pretreatment system; the gas phase from the low-pressure flash zone is sent to a C2 concentrated gas compressor system; and the gas phase from the desorption tower is mixed with the gas phase obtained from the low-pressure flash zone and sent to an ethylene cracking furnace as a C2 concentrated gas product, most of the liquid phase is returned to the multi-stage absorption tower.

Systems and methods for producing a decarbonized blue hydrogen gas for cracking operations utilizing a standard separation process, such as Pressure Swing Absorption (PSA), to separate a tail gas mixture of hydrogen and hydrocarbons into hydrogen gas and a PSA effluent that is used in a hydrogen generation unit to produce the decarbonized blue hydrogen gas for cracking operations

A process for producing hydrocarbons includes providing a component mixture containing hydrocarbons and a feed mixture containing hydrocarbons having two or more carbon atoms and lower boiling compounds using a portion of the component mixture, and forming a heavy fraction and a light fraction using the feed mixture. The heavy fraction contains a portion of the hydrocarbons from the feed mixture and is at least poor in the lower boiling components. The light fraction contains a portion of the lower boiling components from the feed mixture and is at least poor in the hydrocarbons from the feed mixture. The heavy fraction and a first intermediate fraction are formed using some of the feed mixture in low-temperature separation. Some of the first intermediate fraction is subjected to non-cryogenic separation while obtaining the light fraction and a second intermediate fraction. A portion of the second intermediate fraction is recycled to the process.