Synthesizing methanol from a synthesis gas and separating an unreacted gas from a reaction mixture obtained by passing through the synthesis step, the method including a synthesis loop having at least two synthesis steps and at least two separation steps; obtaining a first mixed gas by increasing through a circulator a pressure of a residual gas, obtained by removing a purge gas from the final unreacted gas separated from the final reaction mixture subsequent to the final synthesis step, and by mixing the residual gas with a fraction of a make-up gas; synthesizing methanol; separating a first unreacted gas from the first reaction mixture obtained in the synthesizing step; obtaining a second mixed gas by mixing the first unreacted gas and a fraction of the make-up gas; finally synthesizing methanol; and separating the final unreacted gas from the final reaction mixture obtained in the final synthesis step.

The present invention relates to a saturator. The present invention further relates to a method for reusing a waste water stream from a Fischer-Tropsch reactor. The invention further relates to system for recycling waste water from a Fischer-Tropsch reactor preferably within a gas-to-liquids (GTL) plant.

An apparatus for addition of droplets of a monomer solution for production of poly(meth)acrylate to a reactor for droplet polymerization, comprising at least one channel or a dropletizer head having, at its base, holes through which the solution is dropletized into the reactor, at least one of the following features being fulfilled: (a) the ratio of the area covered by the channels or the dropletizer head in the reactor relative to the area which is defined by the circumference of a line along the outermost holes is less than 50%, (b) the number of holes relative to the area which is defined by the circumference of a line along the outermost holes is within a range from 100 to 1000 holes/m.sup.2.

A method of forming a hydrocarbon product, the method comprising a first step of enriching a carrier liquid with carbon monoxide and hydrogen and a subsequent step of bringing the enriched carrier liquid into contact with a catalyst in a first reaction zone of a reactor, wherein the catalyst catalyzes reaction of the carbon monoxide and hydrogen to form the hydrocarbon product.

The present invention relates to a fluidized bed reactor, comprising a reaction tube, a distributor and a heating device, the reaction tube and the distributor at the bottom of the reaction tube composing a closed space, the distributor comprising a gas inlet and a product outlet, and the reaction tube comprising a tail gas outlet and a seed inlet at the top or upper part respectively, characterized in that the reaction tube comprises a reaction inner tube and a reaction outer tube, and the heating device is an induction heating device placed within a hollow cavity formed between the external wall of the reaction inner tube and the internal wall of the reaction outer tube, wherein the hollow cavity is filled with hydrogen, nitrogen or inert gas for protection, and is able to maintain a pressure of about 0.01 to about 5 MPa; and also to a process of producing high purity granular polysilicon using the reactor. The fluidized bed reactor according to the present invention uses induction heating to heat directly the silicon particles inside the reaction chamber, such that the temperature of the reaction tube is lower than that inside the reaction chamber, which accordingly avoids deposition on the tube wall and results in more uniform heating, and thus is useful for large diameter fluidized bed reactors with much increased output for a single reactor.

The invention relates to a method and to a plant for chemical looping oxidation-reduction combustion (CLC) of a gaseous hydrocarbon feed, for example natural gas essentially containing methane. According to the invention, catalytic steam reforming of the feed is performed between two successive feed combustion steps on contact with an oxidation-reduction active mass in form of particles. The reforming catalyst is arranged in a fixed bed in an intermediate reforming zone (130) between the two reduction zones (120, 140) where the two combustion steps are conducted.

FIG. 2 to be published.

A reactor comprises a reactor vessel defining a confined reactor volume, a support assembly extending about a periphery of the confined reactor volume, a basket positioned within the reactor vessel and supported by the support assembly, the basket having an interior surface and an exterior surface, a downflow zone being defined between the exterior surface of the basket and an interior surface of the confined reactor volume, an inlet screen positioned adjacent to one end of the interior surface and an outlet screen positioned adjacent to an opposite end of the interior surface, an upflow zone defined between the inlet screen and outlet screen, the inlet screen and the outlet screen containing a quantity of particulate catalyst, and a circulating device positioned above said upflow zone and configured to continuously circulate fluid upwardly though said upflow zone and downwardly through said downflow zone, the support assembly and the basket configured to promote the formation of a fluid vortex within a portion of the downflow zone.

A radial flow reactor is described. It includes a vertically extending vessel, an outer conduit, and a central conduit. At least a portion of the outer conduit and the central conduit comprises a screen. A particle retaining space is defined by at least one of the vessel, the central conduit, and the outer conduit, and it communicates with the screen of the outer conduit and the central conduit. An inlet distribution ring is positioned on the outer conduit. The inlet distribution ring comprises a ring having at least one opening and at least one vertically extending riser tube. One end of the riser tube is sealed to the ring, and the other end is positioned inside the outer conduit.

A fluidized bed biogasifier is provided for gasifying biosolids. The biogasifier includes a reactor vessel and a feeder for feeding biosolids into the reactor vessel at a desired feed rate during steady-state operation of the biogasifier. A fluidized bed in the base of the reactor vessel has a cross-sectional area that is proportional to at least the fuel feed rate such that the superficial velocity of gas is in the range of 0.1 m/s (0.33 ft/s) to 3 m/s (9.84 ft/s). In a method for gasifying biosolids, biosolids are fed into a fluidized bed reactor. Oxidant gases are applied to the fluidized bed reactor to produce a superficial velocity of producer gas in the range of 0.1 m/s (0.33 ft/s) to 3 m/s (9.84 ft/s). The biosolids are heated inside the fluidized bed reactor to a temperature range between 900° F. (482.2° C.) and 1700° F. (926.7° C.) in an oxygen-starved environment having a sub-stoichiometric oxygen level, whereby the biosolids are gasified.

An improved reactor comprising a shell and at least one reactor internal component. The reactor internal component includes a tube bundle comprising a plurality of tubes attached by at least one tube support plate comprising at least one radial strut and at least one bracket configured to secure to at least one tube of the tube bundle. The tubes are arranged in concentric bands about a longitudinal axis of the reactor. The reactor comprises a gas inlet plate, a catalyst support plate, and a top plate.