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 device for indicating elapsed time by way of the state of indicators is disclosed, such indicators being arranged in at least four groups such that the first two groups taken together indicate elapsed hours and the second two groups taken together indicate elapsed minutes. The indicators are switchable between a first and second state, such as illuminated or not illuminated. The number of indicators in a first state, such as illuminated, indicate the value of a digit.

Abstract: Disclosed are compliant variable tension risers (106) to connect deep-water subsea wellheads (102) to a single floating platform (104) in wet tree or dry try systems. The variable tension risers (106) allow several subsea wellheads (102), 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 (104). Also disclosed are methods to counter buoyancy and install variable tension risers using a weighted chain ballast line (228, 230).

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: A pipeline segment 5, used for the manufacture of a thin-walled underwater pipeline 50, is disclosed. Terminal pipe sections 20 are at either end of main pipe section 10. Terminal pipe sections 20 are thick-walled or otherwise resistant to collapse due to external pressure. A pressure isolation device 30 maintains an internal pressure in main pipe section 10 above a shutoff pressure. A pressure compensation system 35 can protect main pipe section 10 from collapse due to external pressure. Pipeline segments 5 can be manufactured by connecting and winding stalks 100 onto storage device 110 forming main pipe section 10. Terminal pipe section 20 can be connected to the lead end of main pipe section 10, and main pipe section 10 can be unwound from storage device 110 while towing.

Abstract: A process for the selective hydrogenation of alpha-methyl-styrene (AMS) to cumene in a two catalyst system is disclosed. A crude cumene feed stream containing up to 10% AMS by weight is supplied to the first reaction zone 112 and mixed with hydrogen in a first catalyst bed 118 containing a nickel catalyst, converting from 70 to 95 percent of the AMS to cumene. Cumene and remaining AMS are separated from hydrogen in a liquid take off tray 120. The first reaction zone 112 5effluent is supplied to a second reaction zone 114, where the effluent and hydrogen gas are mixed in a second catalyst bed 126 containing a noble-metal catalyst to substantially convert any remaining AMS to cumene. Cumene is collected, separated from the hydrogen, and can be resupplied to the hydrogenation reactor 110, or supplied as feed to a phenol synthesis loop.

Abstract: An ammonia converter system 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: Various apparatuses and methods to traverse an undersea topographic feature (12) with a subsea pipeline (18) are disclosed. The apparatuses and methods of the present invention accomplish this task through the use of a concentrated buoyancy scheme (10). The invention disclosed can allow more efficient and cost effective traversal of hostile terrain for subsea pipelines at great depths while minimizing the risk of rupturing the pipeline (18) or negatively impacting the surrounding undersea environment.

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: Various apparatuses and methods to traverse an undersea topographic feature (12) with a subsea pipeline (18) are disclosed. The apparatuses and methods of the present invention accomplish this task through the use of a concentrated buoyancy scheme (10). The invention disclosed can allow more efficient and cost effective traversal of hostile terrain for subsea pipelines at great depths while minimizing the risk of rupturing the pipeline (18) or negatively impacting the surrounding undersea environment.

Abstract: A method and system for recovering fines from a light FCC-type effluent gas. Cracked gases from the reactor are cooled by direct contact with circulating oil in an oil quench tower. The circulating oil also washes out the catalyst fines carried with the reactor effluent gas. A flow of the oil from the quench tower bottoms is sent through one of a pair of filters to remove fines and recycled to the tower. The other filter is in backwash operation using a compressed gas to remove the fines therefrom and into a surge drum. Fuel oil or quench oil is added to the drum to form a slurry, which carries the catalyst fines to the regenerator where the oil is combusted to supply the FCC system heat requirements. Since a minimum amount of fuel oil is generated in the FCC, fuel oil is imported to inventory the quench tower.

Abstract: Apparatus and method are provided for separating and stripping suspensions comprising catalyst particles transported in vapors from the fluid catalytic cracking riser/reactor. Particles are disentrained from vapor in a vortex zone 112 of the primary cyclonic separator 100. The disentrained particles enter a stripping zone 126, wherein the particles are contacted with a stripping gas 136 to recover vapors entrained and adsorbed onto the catalyst. The stripping gas 136 enters stripping zone 126 via perforations in the wall of the cyclone 100. The stripping gas 136 limits the residual catalytic conversion of hydrocarbon vapors and formation of delta-coke on the catalyst. Stripped catalyst is delivered from the cyclone stripping zone 126 via a dipleg 130 connected to a bottom of the cyclone 100, and enters an FCC stripping vessel. Solids-lean stripping gas and vapors from the catalyst particles are blended with the carrier fluid and discharged from the cyclone.

Abstract: Disclosed is a process for the upgrading and demetallizing of heavy oils and bitumens. A crude heavy oil and/or bitumen feed is supplied to a solvent extraction process 104 wherein DAO and asphaltenes are separated. The DAO is supplied to an FCC unit 106 having a low conversion activity catalyst for the removal of metals contained therein. The demetallized distillate fraction is supplied to a hydrotreater 110 for upgrading and collected as a synthetic crude product stream. The asphaltene fraction can be supplied to a gasifier 108 for the recovery of power, steam and hydrogen, which can be supplied to the hydrotreater 110 or otherwise within the process or exported. An optional coker 234 can be used to convert excess asphaltenes and/or decant oil to naphtha, distillate and gas oil, which can be supplied to the hydrotreater 220.

Abstract: Disclosed are compliant variable tension risers (106) to connect deep-water subsea wellheads (102) to a single floating platform (104). The variable tension risers (106) allow several subsea wellheads (102), 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 (104). Also disclosed are methods to counter buoyancy and install variable tension risers using a weighted chain ballast line (228, 230).

Abstract: A process for deethanizing light hydrocarbons comprising olefins is disclosed. A feed stream, comprising ethylene, ethane, propylene, and propane, is supplied to a primary deethanizer 24, having absorption and stripping sections. The absorption section produces an overhead vapor effluent 128, consisting primarily of ethylene and ethane, which is supplied to a C2 splitter to separate ethane and ethylene. The stripping section produces a primary deethanizer bottoms stream having an ethane concentration from 1 to 20 mole percent of the feed ethane. The primary deethanizer bottoms 120 are cooled and supplied to a secondary deethanizer 142 having absorption and stripping sections. The absorption section is refluxed, producing an overhead effluent 154 essentially free of ethylene. The stripping section is refluxed to produce a secondary deethanizer bottoms stream essentially free of ethane. The secondary deethanizer bottoms stream is supplied to a depropanizer or C3 splitter for separation of the remaining olefins.

Abstract: An electric fish barrier for deterring fish from entering a water intake in a reservoir or along a waterway has a set of conductive members at a first voltage potential and a second set of conductive members at a second voltage potential. The conductive members are disposed on support piles extending up from the bottom of the reservoir. Each conductive member extends vertically between a pre-determined range of depths from an upper depth to a lower depth, forming a contiguous voltage gradient between the two sets of conductive members. Fish are drawn to the attraction flow of water flowing into the intake. The two sets of conductive members are oriented such that the attraction flow passes through the contiguous voltage gradient, thereby deterring the fish from following the attraction flow into the water intake.

Abstract: Method and apparatus for contacting two liquid phases for liquid-liquid extraction in a vertical extraction vessel. A relatively heavier liquid phase, descending the extraction vessel at a relatively low volumetric flow rate, is dispersed into a continuous phase comprising a relatively lighter liquid rising through the extraction vessel at a relatively high flow rate. Sieve trays are provided with adjustable active areas and overlapping manways for personnel access.

Abstract: Residual oil supercritical extraction (ROSE) 10 and integrated gasification combined-cycle (IGCC) power systems 70, 114 are cooperatively integrated. High-level heat from the IGCC is used via a heat transfer fluid 84 for high level process heating requirements in the ROSE unit. This can eliminate the fired heater normally required in the ROSE unit, and reduces the size of the gasifier 62 waste heat boiler 72 and/or the high-pressure steam coil 134 and steam turbine generator 144 in the IGCC.

Abstract: Integration of gas oil and light olefin catalytic cracking zones with a pyrolytic cracking zone to maximize efficient production of petrochemicals is disclosed. Integration of the units in parallel allows production of an overall product stream with maximum ethylene and/or propylene by routing various feedstreams and recycle streams to the appropriate cracking zone(s), e.g. ethane/propane to the steam pyrolysis zone and C4 C6 olefins to the light olefin cracking zone. This integration enhances the value of the material balances produced by the integrated units.