Abstract: Methods and apparatus are arranged to increase thermal efficiency, reduce waste water treatment, reduce net usage of fresh water, and improve operational reliability during direct hydrothermal upgrading of carbonaceous materials, including low-rank coals. Drain water collected from the hydrothermal upgrading system is passed through a reboiler system to generate steam which can be returned to the hydrothermal processor system for use therein.

Abstract: A structure for the destruction of dangerous materials is described which has a destruction location, which may be a pit below ground level. The destruction pit contains the dangerous materials. At least one durable, sealed membrane is present beneath at least a portion of the destruction pit. An overburden mound of soil is provided above the destruction pit; and at least one shaped explosive charge placed adjacent the dangerous materials capable of subjecting the dangerous materials to crushing detonation forces and high heat for a period of time. After detonation of the explosive charge to destroy the dangerous materials and their containers, such as by pyrolysis, the destruction pit is remediated by removal of the waste products.

Abstract: A method and apparatus for removing light hydrocarbons, such as heptane, from coal agglomerates includes an enclosed chamber having a substantially horizontal perforate surface therein. The coal agglomerates are introduced into a water bath within the chamber. The agglomerates are advanced over the surface while steam is substantially continuously introduced through the surface into the water bath. Steam heats the water and causes volatilization of the light hydrocarbons, which may be collected from the overhead of the chamber. The resulting agglomerates may be collected at the opposite end from the surface and subjected to final draining processes prior to transportation or use.

Abstract: Apparatus and method for handling geothermal brine containing high non-condensible gas concentrations. The brine is directed into a pre-flash chamber where a vapor fraction is separated from a liquid fraction, the vapor fraction including steam and a non-condensible gas. The vapor fraction is directed into and through a reboiler in countercurrent flow relationship to a condensate. This action causes the steam of the vapor fraction to be stripped from the non-condensible gas and also causes the condensate to be heated by the steam. The non-condensible gas flows out of the reboiler to a gas expander collection station, or to the atmosphere while the condensate flows to a first flash chamber where it flashes to obtain clean steam for driving a first work producing apparatus, such as a turbine. The condensate from the first flash chamber is partially returned by a pump to a condensate inlet of the reboiler to form a closed system.

Abstract: Efficient removal of sulfur dioxide from a flue gas stream is achieved in a scrubber using a recirculating aqueous stream containing magnesium hydroxide and magnesium sulfite which together act as SO.sub.2 absorbents. Magnesium sulfite is derived from magnesium hydroxide, which is the product of a reaction between soluble magnesium from the seawater and calcium hydroxide added to the scrubbing system. Magnesium sulfite and bisulfite are oxidized to magnesium sulfate by the introduction of air. Magnesium sulfate is converted back to magnesium hydroxide by reaction with additional calcium hydroxide, with gypsum as a by-product. Gypsum is soluble in large amounts of seawater and may be returned to the ocean without adverse environmental impact.

Abstract: A process for preparing coal for use as a fuel. Forming a coal-water slurry having solid coal particles with a particle size not exceeding about 80 microns, transferring the coal-water slurry to a solid bowl centrifuge, and operating same to classify the ground coal-water slurry to provide a centrate containing solid particles with a particle size distribution of from about 5 microns to about 20 microns and a centrifuge cake of solids having a particle size distribution of from about 10 microns to about 80 microns. The classifer cake is reground and mixed with fresh feed to the solid bowl centrifuge for additional classification.