Abstract: Systems and processes for adjusting hydrogen content of a synthesis gas are provided. At least a portion of carbon monoxide in a syngas can be converted to carbon dioxide to provide a shifted syngas and condensed water. The syngas can have a first hydrogen to carbon monoxide ratio and a first temperature, and the shifted syngas can have a second hydrogen to carbon monoxide ratio and a second temperature, both greater than the first. Heat from the shifted syngas can be at least partially transferred from the shifted syngas to the condensed water to at least partially vaporize the condensed water. The syngas can be at least partially saturated with the at least partially vaporized condensed water. A ratio of the water vapor to syngas can be about 1.0 or less.

Abstract: Systems and methods for producing ammonia. The system can include a first shell having two or more discrete catalyst beds disposed therein, a second shell disposed about the first shell, a first heat exchanger disposed external to the first shell and in fluid communication therewith, a second heat exchanger disposed external to the second shell and in fluid communication therewith, and a flow path disposed within the first shell. A first portion can be reacted in the presence of the catalyst to provide an ammonia effluent. The heat of reaction from the ammonia effluent can be exchanged within the first heat exchanger and the second heat exchanger. The heated second portion of the feed gas can be introduced to the first shell and can be reacted in the presence of the catalyst.

Abstract: An ammonia converter and method are disclosed. The reactor can alter the conversion of ammonia by controlling the reaction temperature of the exothermic reaction along the length of the reactor to parallel the equilibrium curve for the desired product. The reactor 100 can comprise a shell 101 and internal catalyst tubes 109. The feed gas stream enters the reactor, flows through the shell 101, and is heated by indirect heat exchange with the catalyst tubes 109. The catalyst tubes 109 comprise reactive zones 122 having catalyst and reaction limited zones 124 that can comprise inert devices that function to both separate the reactive zones, increase heat transfer area, and reduce the temperature of the reaction mixture as the effluent passes through the catalyst tube 109.

Abstract: An ammonia converter is disclosed. The converter can alter the conversion of ammonia by controlling the reaction temperature of the exothermic reaction along the length of the reactor to parallel the equilibrium curve for the desired product. The converter can comprise a shell 101 and internal catalyst tubes 109. The feed gas stream enters the reactor, flows through the shell 101, and is heated by indirect heat exchange with the catalyst tubes 109. The catalyst tubes 109 comprise reactive zones 122 having catalyst and reaction limited zones 124 that can comprise inert devices that function to both separate the reactive zones, increase heat transfer area, and reduce the temperature of the reaction mixture as the effluent passes through the catalyst tube 109.

Abstract: Systems and methods for staging an investment in hydrocarbon processing are provided. In a first stage, a hydrocarbon feed can be apportioned equally or unequally into first and second portions. The first portion can be mixed with one or more oxidants and gasified to provide a first effluent, at least a portion of which can be combusted to provide steam. The second portion can be mixed with one or more solvents to provide one or more fungible hydrocarbon products, at least a portion of which can be sold to generate capital. In a second stage, the hydrocarbon feed can be mixed with one or more solvents and one or more non-catalytic solids and the resultant mixture thermally cracked to provide one or more hydrocarbon products and coked non-catalytic solids. The coked, non-catalytic solids can be regenerated and recycled.

Abstract: A process for increasing ethylene yield in a cracked hydrocarbon is provided. A hydrocarbon feed stream comprising at least 90% by weight of one or more C4-C10 hydrocarbons can be heated to provide an effluent stream comprising at least 10% by weight propylene. The effluent stream can be selectively separated to provide a first stream comprising heavy naphtha, light cycle oil, slurry oil, or any combination thereof and a second stream comprising one or more C4-C10 hydrocarbons. The second stream can be treated to remove oxygenates, acid gases, water, or any combination thereof to provide a third stream comprising the one or more C4-C10 hydrocarbons. The third stream can be selectively separated to provide a product stream comprising at least 30% by weight propylene. At least a portion of the product stream can be recycled to the hydrocarbon feed stream to increase ethylene yield in the effluent stream.

Abstract: Apparatuses including a subsea pipeline (18) extending from a first location (14) to a second location (16) and including at least one distributed buoyancy region (102) to traverse a seabed topographic feature (12) are presented. Methods including laying a subsea pipeline (218) including laying a negatively buoyant section of pipeline (218A), a distributed buoyancy section (202) of pipeline (218), and a second negatively buoyant section of pipeline (218B) from a pipelay vessel (220) to traverse an undersea topographic feature (212) are also presented.

Abstract: A submersible process environment for sub-sea processing is provided. Such environment can include a modular encapsulated unit having an interior volume and one or more processing units disposed therein, a first valve in fluid communication with the interior and exterior of the unit, and a second valve in fluid communication with the interior and exterior of the unit. The first valve and the second valve can be in fluid communication with the processing unit, and the processing unit can receive a fluid from the first valve and discharges the fluid to the second valve.

Abstract: Disclosed is a process for the upgrading of heavy oils and bitumens, where the total feed to the process can include heavy oil or bitumen, water, and diluent. The process can include the steps of solvent deasphalting 110 the total feed 105 to recover an asphaltene fraction 116, a deasphalted oil fraction 118 essentially free of asphaltenes, a water fraction 112, and a solvent fraction 114. The process allows removal of salts from the heavy oils and bitumens either into the aqueous products or with the asphaltene product.

Abstract: The current subject matter relates to compliant variable tension risers to connect deep-water subsea wellheads to a single floating platform in wet tree or dry try systems. The variable tension risers allow several subsea wellheads, in water depths from 1220 to 3050 meters, at lateral offsets from one-tenth to twice the depth or more, to tie back to a single floating platform. Also, the current subject matter relates to methods to counter buoyancy and install variable tension risers using a weighted chain ballast line.

Abstract: A process for producing electrical power, chemicals, carbon dioxide, and hydrogen is provided. One or more feedstocks and one or more oxidants can be combined in a fluidized reaction zone heated to a temperature from about 1050° F. to about 1900° F. to provide a synthesis gas comprising carbon dioxide, carbon monoxide and hydrogen. In one or more embodiments, at least a portion of the synthesis gas can be used as a fuel source for one or more turbines to drive one or more electrical generators. In one or more embodiments, at least a portion of the synthesis gas can be introduced to one or more gas converters to provide methanol, alkyl formates, dimethyl ether, ammonia, Fischer-Tropsch products, derivatives thereof or combinations thereof.

Abstract: Two or more cyclone systems can be contained in a single vessel. Each cyclone system can be in fluid communication with an inlet stream and a fluid discharge line. First cyclone system can include a vent open to the cyclone containing vessel. Second cyclone system can be sealed to restrict fluid entry from and/or exit into vessel, which can inhibit product vapors from exiting the vent of one cyclone system into the vessel and flowing into the vent of the other cyclone system.

Abstract: Systems and methods for producing urea are provided. A method for producing urea can include exchanging heat from a syngas comprising hydrogen and carbon dioxide to a urea solution comprising urea and ammonium carbamate. The heat transferred can be sufficient to decompose at least a portion of the ammonium carbamate. In one or more embodiments, the syngas can be reacted with liquid ammonia to provide a carbon dioxide lean syngas and an ammonium carbamate solution. The ammonium carbamate solution can be heated to a temperature of about 180° C. or more. At least a portion of the ammonium carbamate in the heated ammonium carbamate solution can be dehydrated to provide the urea solution.

Abstract: Low-energy, low-capital hydrogen production is disclosed. A reforming exchanger 14 is placed in parallel with an autothermal reformer (ATR) 10 to which are supplied a preheated steam-hydrocarbon mixture. An air-steam mixture is supplied to the burner/mixer of the ATR 10 to obtain a syngas effluent at 650°-1050° C. The effluent from the ATR is used to heat the reforming exchanger, and combined reformer effluent is shift converted and separated into a mixed gas stream and a hydrogen-rich product stream. High capital cost equipment such as steam-methane reformer and air separation plant are not required.

Abstract: Disclosed are methods to counter buoyancy and install variable tension risers using a weighted chain ballast line. An example of an apparatus used in conjunction with the embodiments includes compliant variable tension risers to connect deep-water subsea wellheads to a single floating platform. The variable tension risers allow several subsea wellheads, in water depths from 4,000 to 10,000 feet, at lateral offsets from one-tenth to one-half of the depth, to tie back to a single floating dry tree semi-submersible platform.

Abstract: Ammonia is produced in a reactor in which pseudoisothermal conditions can be approached by convective cooling of a reaction zone of the reactor by positioning at least a portion of the reaction zone in indirect contact with a flow of hot gas such as exhaust gas or preheated air. The hot gas may be supplied from a fired heater, a boiler, a reformer, a process air preheat furnace, a gas turbine, or the like. The reactor converts a feed stream of a purge gas or syngas to ammonia. The method may be implemented in a primary synthesis loop or in a purge gas loop of a new ammonia plant, or by retrofitting an existing ammonia plant. Cooperatively installed with a primary ammonia synthesis loop, the reactor increases total ammonia production.

Abstract: A dual riser FCC process is disclosed wherein first and second hydrocarbon feeds (5, 6) are supplied to the respective first and second risers (2, 4) to make an effluent rich in ethylene, propylene and/or aromatics. Where the hydrocarbon feeds are different, the respective risers can have different conditions to favor conversion to ethylene and/or propylene. A minor amount of a coke precursor (80, 82) can be added to one or both of the hydrocarbon feeds (5, 6) to reduce or eliminate the amount of supplemental fuel needed to heat balance the system. The different feeds, including the coke precursor and any recycle streams (36, 44) can be segregated by type to improve olefin yields, including an embodiment where the paraffinic feeds are supplied to one riser and the olefinic feeds to the other.

Abstract: Self purging expansion joint can include first annular seal sleeve connecting bellows to first conduit and second annular seal sleeve connecting bellows to second conduit. Flow-restricting orifice(s) can allow a higher pressure external fluid to flow through the annular passage to purge the bellows and into the primary fluid flow passage of the expansion joint containing a lower pressure fluid. Self purging expansion joint can be utilized in a disengager vessel of a fluid catalytic cracking (FCC) unit, for example, between primary and secondary stripping cyclones.

Abstract: Pipe shoe can include pipe retained by clamp attached to top plate. Acoustic isolation block is disposed for compression between top plate and bottom plate. Top plate is retained to bottom plate by stud(s) and nut(s). Flexible peripheral seal is disposed around acoustic isolation block between top and bottom plates. Pipe shoe can include thermal insulation and/or protective covering over any portion of pipe shoe and/or hot pipe.

Abstract: Ammonia is produced in a reactor 22, 24, 246, 248, 250 or 252, in which pseudoisothermal conditions can be approached by convective cooling of a reaction zone of the reactor by positioning at least a portion of the reaction zone in indirect contact with a flow of hot gas such as exhaust gas 18 or preheated air. The hot gas 18 may be supplied from a fired heater, a boiler 10, a reformer 202, a process air preheat furnace, a gas turbine, or the like. The reactor converts a feed stream of a purge gas 12 or syngas to ammonia. The method may be implemented in a primary synthesis loop (as at 246, 248, 250, 252) or in a purge gas loop 12 of a new ammonia plant, or by retrofitting an existing ammonia plant. Cooperatively installed with a primary ammonia synthesis loop, the reactor increases total ammonia production.