A process for the manufacture of a useful product from carbonaceous feedstock of fluctuating compositional characteristics, comprising the steps of: continuously providing the carbonaceous feedstock of fluctuating compositional characteristics to a gasification zone; gasifying the carbonaceous feedstock in the gasification zone to obtain raw synthesis gas; recovering at least part of the raw synthesis gas from the gasification zone and supplying at least part of the recovered raw synthesis gas to a partial oxidation zone; equilibrating the H.sub.2:CO ratio of the raw synthesis gas in the partial oxidation zone to obtain equilibrated synthesis gas; recovering at least part of the equilibrated synthesis gas from the partial oxidation zone and treating the gas to remove impurities and generate a fine synthesis gas; and converting the optionally adjusted fine synthesis gas into the useful product in a further chemical reaction requiring a usage ratio.

The invention relates to a gas scrubbing process and a corresponding plant for removal of acidic gas constituents from crude synthesis gas which make it possible by treatment of shifted and of unshifted crude synthesis gas in the gas scrubbing process and by combination of the thus-obtained partial product streams to produce a plurality of gas products having different compositions. In addition, the invention ensures that the flash gases obtained during decompression of the laden scrubbing medium are utilized materially and/or energetically in advantageous fashion.

The invention relates to a gas scrubbing process and a corresponding plant for removal of acidic gas constituents from crude synthesis gas which make it possible by treatment of shifted and of unshifted crude synthesis gas in the gas scrubbing process and by combination of the thus-obtained partial product streams to produce a plurality of gas products having different compositions. In addition, the invention ensures that the flash gases obtained during decompression of the laden scrubbing medium are utilized materially and/or energetically in advantageous fashion.

A process to efficiently convert organic feedstock material into liquid non-oxygenated hydrocarbons in the C.sub.5 to C.sub.12 carbon skeleton range is disclosed. The process can utilize gaseous, liquid or solid organic feedstocks containing carbon, hydrogen and, optionally, oxygen. The feedstock may require preparation of the organic feedstock for the process and is converted first into a synthesis gas containing carbon monoxide and hydrogen. The synthesis gas is then cleaned and conditioned and extraneous components removed, leaving substantially only the carbon monoxide and hydrogen. It is then converted via a series of chemical reactions into the desired liquid hydrocarbons. The hydrocarbons are suitable for combustion in a vehicle engine and may be regarded a replacement for petrol made from fossil fuels in the C.sub.5 to C.sub.2 carbon backbone range. The process also recycles gaseous by-products back through the various reactors of the process to maximize the liquid hydrocarbon in the C.sub.5 to C.sub.12 carbon skeleton range yield.

A process to efficiently convert organic feedstock material into liquid non-oxygenated hydrocarbons in the C.sub.5 to C.sub.12 carbon skeleton range is disclosed. The process can utilize gaseous, liquid or solid organic feedstocks containing carbon, hydrogen and, optionally, oxygen. The feedstock may require preparation of the organic feedstock for the process and is converted first into a synthesis gas containing carbon monoxide and hydrogen. The synthesis gas is then cleaned and conditioned and extraneous components removed, leaving substantially only the carbon monoxide and hydrogen. It is then converted via a series of chemical reactions into the desired liquid hydrocarbons. The hydrocarbons are suitable for combustion in a vehicle engine and may be regarded a replacement for petrol made from fossil fuels in the C.sub.5 to C.sub.2 carbon backbone range. The process also recycles gaseous by-products back through the various reactors of the process to maximize the liquid hydrocarbon in the C.sub.5 to C.sub.12 carbon skeleton range yield.

A system is disclosed. The system can store a fuel reagent such as methanol for conversion into hydrogen to power one or more facility systems via a backup power system. A reactor controller can monitor a power demand of the one or more facility systems and determine whether the power demand is met by a primary power system. The fuel reagent can be provided to a fuel reactor in response to the reactor controller determining that the one or more facility systems are operating at a power deficit to generate an amount of hydrogen that, when provided to the backup power system, causes the backup power system to generate an amount of power that meets or exceeds the power deficit.

A system is disclosed. The system can store a fuel reagent such as methanol for conversion into hydrogen to power one or more facility systems via a backup power system. A reactor controller can monitor a power demand of the one or more facility systems and determine whether the power demand is met by a primary power system. The fuel reagent can be provided to a fuel reactor in response to the reactor controller determining that the one or more facility systems are operating at a power deficit to generate an amount of hydrogen that, when provided to the backup power system, causes the backup power system to generate an amount of power that meets or exceeds the power deficit.

A system for combined production of yellow phosphorous and syngas is disclosed. The air separation unit, the pulverized coal preparation unit and the mineral aggregate forming unit are respectively connected to a gas inlet and a top feeding port of the phosphorus coal gasifier; phosphorus-containing syngas obtained from phosphorus coal gasifier is connected to a gas inlet of the separating washing unit through an outlet of the phosphorous coal gasifier; Yellow phosphorus products and crude syngas are respectively output from the output port of the separating washing unit; and then the crude syngas is purified to obtain refined syngas. A slag discharge port at the bottom of the phosphorus coal gasifier is connected to an input port of a slag cold quenching unit. The system can improve the available energy of yellow phosphorous production, the production capacity of yellow phosphorus and the yield of syngas, and reduce CO.sub.2 emission.

A system for combined production of yellow phosphorous and syngas is disclosed. The air separation unit, the pulverized coal preparation unit and the mineral aggregate forming unit are respectively connected to a gas inlet and a top feeding port of the phosphorus coal gasifier; phosphorus-containing syngas obtained from phosphorus coal gasifier is connected to a gas inlet of the separating washing unit through an outlet of the phosphorous coal gasifier; Yellow phosphorus products and crude syngas are respectively output from the output port of the separating washing unit; and then the crude syngas is purified to obtain refined syngas. A slag discharge port at the bottom of the phosphorus coal gasifier is connected to an input port of a slag cold quenching unit. The system can improve the available energy of yellow phosphorous production, the production capacity of yellow phosphorus and the yield of syngas, and reduce CO.sub.2 emission.

Method and plant for generating a synthesis gas which consists mainly of carbon monoxide and hydrogen and has been freed of acid gases, proceeding from a hydrocarbonaceous fuel, and air and steam, wherein low-temperature fractionation separates air into an oxygen stream, a tail gas stream and a nitrogen stream, wherein the tail gas stream and the nitrogen stream are at ambient temperature and the nitrogen stream is at elevated pressure, wherein the hydrocarbonaceous fuel, having been mixed with the oxygen stream and steam at elevated temperature and elevated pressure, is converted to a synthesis gas by a method known to those skilled in the art, and wherein acid gas is subsequently separated therefrom by low-temperature absorption in an absorption column, wherein the nitrogen stream generated in the fractionation of air is passed through and simultaneously cooled in an expansion turbine and then used to cool either the absorbent or the coolant circulating in the coolant circuit of the compression refrigeration plant.