In a novel process for methanol production from low quality synthesis gas, in which relatively smaller adiabatic reactors can be operated more efficiently, some of the inherent disadvantages of adiabatic reactors for methanol production are avoided. This is done by controlling the outlet temperature in the pre-converter by rapid adjustment of the recycle gas, i.e. by manipulating the gas hourly space velocity in the pre-converter.

The invention relates to a fuel processor component for a propylene glycol fuel processor, comprising at least one housing (G) having at least two inlets (E1, E2) and two outlets (A1, A2), wherein there is a multitude of first plates (P1) having a first side (S1) and a second side (S2) and second plates (P2) having a third side (S3) and a fourth side (S4) arranged as a stack in the housing (G), wherein the stacked first and second plates (P1, P2) form at least first cavities (H1) and second cavities (H2), wherein the first inlet (E1) has fluid connection to the first outlet (A1) via first cavities (H1) and the second inlet (E2) has fluid connection to the second outlet (A2) via second cavities (H2).

The invention further relates to a propylene glycol fuel processor.

Disclosed is a method for starting up fluidized reaction apparatus that is used for producing lower olefins from methanol or/and dimethyl ether. Said method includes after heating the catalyst bed of circulating fluidized catalytic reaction apparatus to above 200 C. or 300 C. by using a starting-up auxiliary heat source, feeding methanol or dimethyl ether raw materials to a reactor, whereby heat released by the reaction makes the temperature of the reaction system apparatus increase quickly to a designed temperature, consequently making the system reach normal operation state rapidly. Said method is suitable for starting up an exothermic fluidized catalytic reaction apparatus and can simplify the apparatus and operation, accordingly lowering the cost.

A process for starting a multizone circulating reactor containing no polyolefin particles, comprising the steps of conveying gas through the reactor and the gas recycle line, feeding a particulate material comprising a polymerization catalyst and optionally polyolefin into the reactor, controlling the gas flow in a vertical reactor zone equipped with a throttling valve at the bottom so that the upwards gas velocity in the bottom part of this reaction zone is lower than the terminal free-fall velocity of the particulate material fed into the reactor, and, after the weight of the particulate polyolefin in this reactor zone is higher than the drag force of the upward moving gas, controlling the circulation rate of the polymer particles within the multizone circulating reactor by adjusting the opening of the throttling valve and adjusting the flow rate of a dosing gas.

Steam-hydrocarbon reforming reactor with a reformer tube containing ceramic-supported catalyst pellets and metal foam particles. The ceramic-supported catalyst pellets have a porous support comprising one or more of alumina, calcium aluminate, and magnesium aluminate. The metal foam particles comprise Fe and/or Ni. The ceramic-supported catalyst pellets and metal foam particles may be layered or interspersed.

Method for switching between steady-state and non-steady-state operations of a process for the production of a polymer by polymerization of a monomer in the presence of a comonomer and/or hydrogen. The process includes (a1) at non-steady-state controlling the process based on the ratio of comonomer to monomer in the reactor, and (b1) at steady-state controlling the process based on the flow ratio of comonomer to monomer to the reactor, and/or (a2) at non-steady-state controlling the process based on the ratio of hydrogen to monomer in the reactor, and (b2) at steady-state controlling the process based on the flow ratio of hydrogen to monomer to the reactor.

A process for filtering a liquid stream from a fixed bed reaction zone in order to remove catalyst fines contained in the stream. The effluent stream is passed to a filtering section which may contain at least two filtering vessels. Each filtering vessel includes at least two differently filtering sections, each section designed to collect differently sized particles. If a pressure drop occurs in one of the filtering vessels, it may be taken offline to remove the filtering sections and recover the metal in the particles collected on the filtering sections. The other filtering vessel can remain online to allow the filtering process to be continuous. Metal on the catalyst fines may be recovered.

The present invention relates to a process for shutting-down a tubular reactor (1) for a catalytic gas phase reaction from a reaction temperature, wherein the tubular reactor (1) comprises a plurality of vertically arranged reaction tubes (2), an upper tube sheet (5) and a lower tube sheet (6) which each are connected to upper ends and lower ends of the reaction tubes (2) in a gas-tight manner, and a reactor shell (7) which encloses the plurality of reaction tubes (2) forming a liquid-tight heat transfer space (9), wherein, in operation mode, a substantially anhydrous liquefied salt melt (8) is circulated in the heat transfer space (9), characterized in that water (10) is added to the substantially anhydrous liquefied salt melt (8), obtaining a water-salt mixture (11), while cooling the tubular reactor (1) to a temperature below the solidification temperature of the substantially anhydrous liquefied salt melt (8), such that the water-salt mixture (11) is kept in a liquefied state during the whole cooling step of the tubular reactor (1).

The invention relates to a method for start-up and operation of a Fischer-Tropsch reactor comprising the steps of: (a) providing a reactor with a fixed bed of reduced Fischer-Tropsch catalyst that comprises cobalt as catalytically active metal; (b) supplying a gaseous feed stream comprising carbon monoxide and hydrogen to the reactor, wherein the gaseous feed stream initially comprises a nitrogen-containing compound other than molecular nitrogen in an initial concentration in the range of from 0.1 to 50 ppmv based on the volume of the gaseous feed stream; (c) converting carbon monoxide and hydrogen supplied with the gaseous feed stream to the reactor into hydrocarbons at an initial reaction temperature, wherein the initial reaction temperature is set at a value of at least 200 C. and hydrocarbons are produced at a first yield; (d) maintaining the initial reaction temperature at the set value and maintaining the first yield by decreasing the concentration of the nitrogen-containing compound in the gaseous feed stream supplied to the reactor; (e) optionally increasing the reaction temperature after the concentration of the nitrogen-containing compound in the gaseous feed stream has decreased to a value below 100 ppbv.

A fuel cell module includes a fuel cell stack and FC peripheral equipment. The FC peripheral equipment includes an evaporator. At least one of evaporation pipes of the evaporator connects a water vapor discharge chamber and an inlet of a reformer to form an evaporation return pipe as a passage of water vapor. A raw fuel pipe is inserted into the evaporation return pipe for allowing a raw fuel to flow from the downstream side to the upstream side of the evaporation return pipe.