A large-scale fluidized bed biogasifier provided for gasifying biosolids. The biogasifier includes a reactor vessel with a pipe distributor and at least two fuel feed inlets for feeding biosolids into the reactor vessel at a desired fuel feed rate of more than 40 tons per day with an average of about 100 tons per day 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 targeted 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 operation, biosolids are heated inside the fluidized bed reactor to a temperature range between 900 F. (482.2 C.) and 1600 F. (871.1 C.).

Systems and methods for detecting and controlling bed height in fluidized bed reactors are disclosed. The systems and methods employ a plurality of radiation sources and a detector array located along the outer surface of a fluidized bed reactor.

A universal feeder system that combines with a fluidized bed gasification reactor for the treatment of multiple diverse feedstocks including sewage sludge, municipal solid waste, wood waste, refuse derived fuels, automotive shredder residue and non-recyclable plastics. The invention thereby also illustrates a method of gasification for multiple and diverse feedstocks using a universal feeder system. The feeder system comprises one or more feed vessels and at least one live bottom dual screw feeder. The feed vessel is rectangular shaped having three vertical sides and an angled side of no less than 60 degrees from the horizontal to facilitate proper flow of feedstock material that have different and/or variable flow properties. The feedstocks are transferred through an open bottom chute to a live bottom dual screw feeder and through another open bottom chute to a transfer screw feeder that conveys feedstock to the fuel feed inlets of a gasifier.

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.

A plant or refinery may include equipment such as condensers, regenerators, distillation columns, pumps, slide valves, or the like. Different operating methods may impact deterioration in equipment condition, thereby prolonging equipment life, extending production operating time, or providing other benefits. Mechanical or digital sensors may be used for monitoring equipment to determine whether problems are developing. Specifically, sensors may be used in conjunction with one or more system components to predict and detect slide valve sticking. An operating condition of the plant or refinery may be adjusted to prolong equipment life or avoid equipment failure.

A fluidized bed reactor includes a main shell and a coke control zone shell; the main shell includes an upper shell and a lower shell; the upper shell encloses a gas-solid separation zone, and the lower shell encloses a reaction zone; the reaction zone axially communicates with the gas-solid separation zone; the coke control zone shell is circumferentially arranged on an outer wall of the main shell; the coke control zone shell and the main shell enclose an annular cavity, and the annular cavity is a coke control zone; n baffles are radially arranged in the coke control zone, and the n baffles divide the coke control zone into n coke control zone subzones, where n is an integer; the coke control zone subzones are provided with a coke control raw material inlet; and a catalyst circulation hole is formed in each of n1 of the baffles.

Provided are processes for the formation of electrochemically active materials such as lithiated transition metal oxides that solve prior issues with throughput and calcination. The processes include forming the materials in the presence of a processing additive that includes potassium prior to calcination that produces active materials with increased primary particle grain sizes.

A catalyst composition for the polymerization of propylene is provided. The catalyst composition includes one or more Ziegler-Natta procatalyst compositions having one or more transition metal compounds and one or more esters of aromatic dicarboxylic acid internal electron donors, one or more aluminum containing cocatalysts and a selectivity control agent (SCA). The SCA is a mixture of an activity limiting agent and a silane composition. The catalyst composition has a molar ratio of aluminum to total SCA from 0.5:1 to 4:1. This aluminum/SCA ratio improves polymerization productivity and the polymer production rate. The catalyst composition is self-extinguishing.

A spent catalyst distributor for distributing spent catalyst in a catalyst regenerator vessel housing a dense phase catalyst bed and a dilute phase catalyst bed. The spent catalyst distributor comprises a conduit comprising a proximal end and a distal end. The conduit projects horizontally or horizontally and downwardly into the regenerator vessel and includes an opening located at the distal end for introducing the spent catalyst at a first location inside the regenerator vessel. The conduit further includes a plurality of orifices located along a length of the conduit between the distal end and an inner wall of the regenerator vessel for introducing the spent catalyst at a plurality of locations inside the regenerator vessel.

The present invention relates to a process for determining a set of one or more operating conditions of an olefin polymerization reactor for the synthesis of a polyolefin in slurry condition, comprising the steps of: a1) introducing a polyolefin into a volume of at least one diluent, said diluent being agitated by a powered agitator at a first temperature T1; b1) monitoring the power consumed by the agitator as a function of the concentration, for at least three concentrations C1, C2, and Cn, which are different from each other; c1) repeating steps a1) and b1) at two or more subsequent temperatures T2 and Tn, which are different from each other and from T1; d1) determining from the power consumed by the agitator as a function of concentration, said set of one or more stable operating conditions for the synthesis of the polyolefin in the olefin polymerization reactor.