An integrated plant to generate chemical grade syngas from a steam biomass reforming in a multiple stage bio reforming reactor for use with either a high temperature or low temperature Fischer-Tropsch synthesis process to produce fuel from biomass is discussed. The first stage has a reactor to cause a chemical devolatilization of a biomass feedstock from the biomass feedstock supply lines into its constituent gases of CO, H2, CO2, CH4, tars, chars, and other components into a raw syngas mixture. A second stage performs further reforming of the raw syngas from the first stage into the chemical grade syngas by further applying heat and pressure to chemically crack at least the tars, reform the CH4, or a combination of both, into their corresponding syngas molecules. The second stage feeds the chemical grade syngas derived from the biomass feedstock to the downstream Fischer-Tropsch train to produce the fuel from the biomass. One or more recycle loops supply tail gas or FT product back into the plant.

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.

The present disclosure provides a method for preparing hydrogen-rich gas by solid organics. For example, solid organic raw materials are heated in a pyrolysis reaction device to perform pyrolysis reaction, and gaseous product generated from the pyrolysis reaction performs gasification with steam in a moving bed gasification reaction device to generate hydrogen-rich product. The present disclosure also provides a system for preparing hydrogen-rich gas by solid organics, and the system may include a solid heat carrier grading-dedusting device; a pyrolysis reaction device; a moving bed gasification reaction device; and a riser and combustion reactor. The present disclosure may operate at atmospheric pressure, and the technology is simple and suitable for the gasification and co-gasification of various high-volatile solid organics, such as raw materials containing a relatively large amount of moisture, mineral substance, and sulfur content.

A process for producing black powder oxygen carriers for use in a chemical looping combustion unit includes the steps of: (a) removing and collecting the black powder waste material that was formed in a gas pipeline; (b) pre-treating the collected black powder to adjust its spherical shape to avoid attrition and fines production; and (c) activating the black powder to increase its reactivity rate and produce the black powder oxygen carrier that is suitable for use in the chemical looping combustion process as an oxygen carrier.

The invention relates to a catalyst regeneration process for a tar reforming catalyst within a catalyst bed in a tar reformer. The process comprises the steps of:—Admitting a main gas stream with controlled temperature and oxygen content to an inlet into the tar reformer;—Passing the main gas stream through the catalyst bed to form an oxygen depleted gas stream;—Exiting the oxygen depleted gas stream from the tar reformer; and—Recycling at least a part of the oxygen depleted gas stream exiting from the tar reformer back into said main gas stream upstream said tar reformer. The temperature of said main gas stream at the inlet is controlled to be within the range from about 500° C. to about 1000° C.

Carbonaceous-containing material including biomass, municipal solid waste, and/or coal and/or contaminated soil, and/or other carbonaceous materials may be gasified at low temperatures utilizing a reactor designed to generate shockwaves in a supersonic gaseous vortex. Preprocessed waste may be introduced into the reactor. A gas stream may be introduced substantially tangentially to an inner surface of a chamber of the reactor to generate a gaseous vortex rotating about a longitudinal axis within the chamber. The gas stream may be introduced using a nozzle that accelerates the gas stream to a supersonic velocity, and may impinge on an impactor positioned within the reactor chamber. A frequency of shockwaves emitted from the nozzle into the gaseous vortex may be controlled. The processed waste discharged from the reactor, which may include a gas component and at least a solid component, can be subjected to separation, and at least some of the gas component and at least one solid component (i.e., tars) may be fed back to the feeding device so that the solids from the processed waste condense on preprocessed waste contained in the feeding device and are reprocessed within the reactor. The gas component from the feeding device may be cleaned after the solids have been condensed out in the feeding device.

A cooling wall includes: a wall surface defined by arrangement of central axes of a plurality of cooling tubes; and an opening formed in a part of the wall surface in which a burner is installable, each of the plurality of cooling tubes forming the opening has a straight portion and a curved portion, the plurality of cooling tubes include a first cooling tube whose first virtual axis extending in an axial direction of the straight portion overlaps the opening, and a second cooling tube whose second virtual axis extending in an axial direction of the straight portion is located outside an outer circumference of the opening in a radial direction, the curved portion of the first cooling tube is arranged so as to form a curve along the outer circumference surface of the opening and on a surface along the wall surface.

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains.

A carbonaceous fuel gasification system for a supercritical CO.sub.2 power cycle system includes a micronized char preparation system comprising a devolatilizer that receives solid carbonaceous fuel, hydrogen, oxygen, and fluidizing steam and produces micronized char, steam, hydrogen, and volatiles. An indirect gasifier includes a vessel comprising a gasification chamber that receives the micronized char, a conveying gas, and steam where the gasification chamber provides syngas, ash, and steam. A combustion chamber receives syngas and an oxidant and burns the mixture of syngas with the oxidant to provide heat for gasification and for heating incoming flows, thereby generating steam and CO.sub.2. The heat for gasification is transferred from the combustion chamber to the gasification chamber by circulating refractory sand. A syngas cooler cools the syngas and generates steam and provides to a supercritical CO.sub.2 power cycle system that performs a supercritical CO.sub.2 power cycle for generating power.

The description describes the integration of a gas fermentation process with a gasification process whereby effluent from the gas fermentation process is recycled to the gasification process. The one or more effluents which can be recycled include a stream comprising microbial biomass, a product stream comprising at least a portion of the at least one fermentation product, a by-product stream comprising fusel oil, and a waste water stream comprising microbial biomass. The stream comprising biomass can be dried before it is passed to the gasification zone. At least a portion of the waste water stream can be passed to the gasification process where one use is to replace at least a portion of the process water. The waste water stream can be further processed to produce a clarified water stream and a biogas stream comprising methane either or both of which can be passed to the gasification process.