The present disclosure provides processes for converting a hydrocarbon feedstock to a hydrocarbon product stream. A process may include introducing the hydrocarbon feedstock to a reactor including a catalyst to form a reactor effluent having a temperature of from about 700 F. to about 1300 F. The catalyst may include a crystalline microporous material. The process may also include cooling the reactor effluent to a temperature of from about 350 F. to about 550 F. to form a condensate and a vapor stream. The condensate and vapor stream may be separated in a first separation system. Additionally, the vapor stream may be introduced to a second separation system to form a hydrocarbon product stream and a light hydrocarbon stream. The present disclosure also relates to apparatuses including a reactor, a vapor-liquid separator, a heat exchanger, and a separation system.

A hydrogen production apparatus includes: a first heating furnace including: a first accommodating tank in which a moving bed of a catalyst containing any one or more of iron, nickel, copper, and aluminum is formed; and a heating tube, which is provided in the first accommodating tank, and through which a heat medium passes; a second heating furnace including: a burner that burns fuel to generate an exhaust gas; and a second accommodating tank in which a fluidized bed of the catalyst discharged from the first heating furnace is formed with the exhaust gas; and a furnace for the pyrolysis including a third accommodating tank in which a fluidized bed of the catalyst discharged from the second heating furnace is formed with a raw material gas containing hydrocarbon.

A direct decomposition device for hydrocarbons for directly decomposing hydrocarbons into carbon and hydrogen includes a rector containing a catalyst including a plurality of metal particles with an iron purity of 86% or more. The reactor is configured to be supplied with a raw material gas containing hydrocarbons.

An aspect of the present invention provides an internal and the like. The internal is easily handled and is capable of yielding a satisfactory defoaming effect. An internal (50) is used in a fluidized bed reaction device (1), in which a first material and a second material are brought into contact with each other and reacted with each other. The internal (50) is attached to a ceiling part of the fluidized bed reaction device (1), and includes a plurality of chains (21).

The present invention discloses processes for oligomerizing an olefin feedstock containing C.sub.4 to C.sub.20 alpha olefins using a catalyst system containing a metallocene compound, an organoaluminum compound, and a suspension of a chemically-treated solid oxide. The liquid medium for the suspension of the chemically-treated solid oxide can be an alpha-olefin oligomer product formed by the oligomerization process.

Provided is a fluidized bed reactor (1) that makes it possible to stably measure a temperature distribution in the fluidized bed reactor (1) while no damage is caused to a temperature measuring section. Provided is a fluidized bed reactor (1) configured to generate trichlorosilane by reacting metallurgical grade silicon powder and hydrogen chloride gas, the fluidized bed reactor (1) including: a reaction vessel (10); and a plurality of temperature measuring sections (50), provided on an outer surface of the reaction vessel (10), each for measuring a temperature inside the reaction vessel (10).

A process where external fuel oil is used to wash entrained catalyst from a fluidized-bed propane dehydrogenation reactor effluent, where the fuel oil and catalyst mixture is returned to the reactor to provide the net fuel required for catalyst regeneration. Optionally the fluidized-bed propane dehydrogenation reactor effluent and the fuel oil are contacted in a direct contact inline device before entering a flash zone in the reactor vessel.

A chemical plant or a petrochemical plant or a refinery may include one or more pieces of equipment that process one or more input chemicals to create one or more products. For example, catalytic dehydrogenation can be used to convert paraffins to the corresponding olefin. A delta temperature controller may determine and control differential temperature across the reactor, and use a delta temperature to control a set point for a heater temperature controller. By doing so, the plant may ramp up a catalytic dehydrogenation unit faster and ensure it does not coke up the catalyst and/or foul a screens too quickly. Catalyst activity may be taken into account and allow the plant to have better control over production and run length of the unit.

Provided is a method for producing aromatic hydrocarbons from light alkanes. A light alkane is contacted with catalyst particles in each of reactors, wherein each of the reactors is a fluidized bed reactor arranged in parallel with each other in a furnace. At least a portion of the alkane feed is converted to aromatic hydrocarbons using the catalyst particles, wherein the aromatic hydrocarbons form a part of a reactor effluent stream. The reactor effluent streams from each of the reactors are merged to form a first merged effluent stream. Catalysts particles deactivated through the light alkane conversion are either regenerated inside the reactors or withdrawn from the reactors for regeneration outside the reactors. The furnace comprises multiple furnaces, and the first merged effluent stream from each of the furnaces is further merged with each other to form a second merged effluent stream.

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.