Abstract: A reformer reactor 10 for producing a hydrogen-rich gas includes a first zone 18, a second zone 20, a third zone 22, a fourth zone 24 and a product gas collection space 40. The zones are sequentially adjacent. A flow path P1 is provided for directing flow of a reaction stream in diverging directions from the first zone 18 into the second zone 20, the flow of the reaction stream continuing in the same general diverging directions through the second zone 20 and into and through the third and fourth zones 22, 24. Directing the flow in diverging directions permits flow into and through a zone over more than just a single cross-sectional geometry of the zone or a single cross-section of the flow path transverse to the direction of flows. This configuration can be used to require a lower pressure for flowing the reaction stream so as to reduce the parasitic requirements of the reactor. This configuration can also be used to increase throughput of the reactor.

Abstract: A reformer is disclosed for converting a hydrocarbon fuel into hydrogen gas and carbon dioxide, the reformer having a first tube, a second tube annularly disposed about the first tube, and a third tube annularly disposed about the second tube. The first tube includes a first catalyst, a first tube outlet, and is adapted for receiving a first mixture of steam. The second tube is adapted for receiving a second mixture of an oxygen-containing gas and a second fuel. The third tube is adapted for receiving a first reaction reformate from the first tube and a second reaction reformate from the second tube, and for producing a third reaction reformate.

Abstract: A hydrocarbon fuel reformer (200) is disclosed suitable for producing synthesis hydrogen gas from reactions with hydrocarbons fuels, oxygen, and steam. The reformer (200) comprises first and second tubes (208,218). The first tube (208) includes a first catalyst (214) and receives a first mixture of steam and a first fuel. The second tube (218) is annularly disposed about the first tube (208) and receives a second mixture of an oxygen-containing gas and a second fuel. In one embodiment, a third tube (224) is annularly disposed about the second tube (218) and receives a first reaction reformate from the first tube (208) and a second reaction reformate from the second tube (218). A catalyst reforming zone (260) annularly disposed about the third tube (224) may be provided to subject reformate constituents to a shift reaction. In another embodiment, a fractionator is provided to distill first and second fuels from a fuel supply source.

Abstract: A reformer reactor 10 for producing a hydrogen-rich gas includes a first zone 18, a second zone 20, a third zone 22, a fourth zone 24 and a product gas collection space 40. The zones are sequentially adjacent. A flow path P1 is provided for directing flow of a reaction stream in diverging directions from the first zone 18 into the second zone 20, the flow of the reaction stream continuing in the same general diverging directions through the second zone 20 and into and through the third and fourth zones 22,24. Directing the flow in diverging directions permits flow into and through a zone over more than just a single cross-sectional geometry of the zone or a single cross-section of the flow path transverse to the direction of flows. This configuration can be used to require a lower pressure for flowing the reaction stream so as to reduce the parasitic requirements of the reactor. This configuration can also be used to increase throughput of the reactor.

Abstract: A hydrocarbon fuel reforming method is disclosed suitable for producing synthesis hydrogen gas from reactions with hydrocarbons fuels, oxygen, and steam. A first mixture of an oxygen-containing gas and a first fuel is directed into a first tube 108 to produce a first reaction reformate. A second mixture of steam and a second fuel is directed into a second tube 116 annularly disposed about the first tube 108 to produce a second reaction reformate. The first and second reaction reformates are then directed into a reforming zone 144 and subject to a catalytic reforming reaction. In another aspect of the method, a first fuel is combusted with an oxygen-containing gas in a first zone 108 to produce a reformate stream, while a second fuel under steam reforming in a second zone 116. Heat energy from the first zone 108 is transferred to the second zone 116.

Abstract: An apparatus and a method are disclosed for converting hydrocarbon fuel or an alcohol into hydrogen gas and carbon dioxide. The apparatus includes a first vessel having a partial oxidation reaction zone and a separate steam reforming reaction zone that is distinct from the partial oxidation reaction zone. The first vessel has a first vessel inlet at the partial oxidation reaction zone and a first vessel outlet at the steam reforming zone. The reformer also includes a helical tube extending about the first vessel. The helical tube has a first end connected to an oxygen-containing source and a second end connected to the first vessel at the partial oxidation reaction zone. Oxygen gas from an oxygen-containing source can be directed through the helical tube to the first vessel. A second vessel having a second vessel inlet and second vessel outlet is annularly disposed about the first vessel.

Abstract: A method is disclosed for synthesizing hydrogen gas from hydrocarbon fuel. A first mixture of steam and a first fuel is directed into a first tube 208 to subject the first mixture to a first steam reforming reaction in the presence of a first catalyst 214. A stream of oxygen-containing gas is pre-heated by transferring heat energy from product gases. A second mixture of the pre-heated oxygen-containing gas and a second fuel is directed into a second tube 218 disposed about the first tube 208 to subject the second mixture to a partial oxidation reaction and to provide heat energy for transfer to the first tube 208. A first reaction reformate from the first tube 208 and a second reaction reformate from the second tube 218 are directed into a third tube 224 disposed about the second tube 218 to subject the first and second reaction reformates to a second steam reforming reaction, wherein heat energy is transferred to the third tube 224 from the second tube 218.

Abstract: A method for converting hydrocarbon fuel into hydrogen gas and carbon dioxide within a reformer 10 is disclosed. According to the method, a stream including an oxygen-containing gas is directed adjacent to a first vessel 18 and the oxygen-containing gas is heated. A stream including unburned fuel is introduced into the oxygen-containing gas stream to form a mixture including oxygen-containing gas and fuel. The mixture of oxygen-containing gas and unburned fuel is directed tangentially into a partial oxidation reaction zone 24 within the first vessel 18. The mixture of oxygen-containing gas and fuel is further directed through the partial oxidation reaction zone 24 to produce a heated reformate stream including hydrogen gas and carbon monoxide. Steam may also be mixed with the oxygen-containing gas and fuel, and the reformate stream from the partial oxidation reaction zone 24 directed into a steam reforming zone 26.

Abstract: A thermal expansion valve comprises a metal tube for flowing a fluid therethrough, and a metal rod fixed only at a first end in the tube and disposed wholly within the tube, the metal tube having a greater coefficient of expansion than the metal rod. A plug having an orifice therethrough is disposed in the tube proximate a free end of the rod. Lengthwise thermal expansion and contraction of the tube and the rod caused by the temperature of the fluid in the tube and around the rod causes the free end of the rod to retreat from the plug to increase flow of the fluid therethrough, and causes the free end of the rod to approach the plug to restrict flow of the fluid therethrough, respectively.

Abstract: A thermal expansion valve comprises a metal tube for flowing a fluid therethrough, and a metal rod fixed only at a first end in the tube and disposed wholly within the tube, the metal tube having a greater coefficient of expansion than the metal rod. A plug having an orifice therethrough is disposed in the tube proximate a free end of the rod. Lengthwise thermal expansion and contraction of the tube and the rod caused by the temperature of the fluid in the tube and around the rod causes the free end of the rod to retreat from the plug to increase flow of the fluid therethrough, and causes the free end of the rod to approach the plug to restrict flow of the fluid therethrough, respectively.

Abstract: An improved system for remediating soil contaminated with short-chain hydrocarbons, long-chain hydrocarbons and PCB's. The system includes an rotary drum having first and second heat exchanging regions, each containing separated inner and outer regions. The drum in inclined such that soil fed into the system with a sealed auger for remediation is gravitationally urged through the inner regions whereat thermal energy provided by a burner means, including clamshell ducts, remediates the soil by vaporizing and oxidizing the hydrocarbons and PCB's in a stream of hot gases.

Abstract: Material remediation apparatus includes a remediation drum through which materials, such as soil contaminated with hydrocarbons, are advanced from a feed end to a discharge end of the drum. A tube extending concentrically from the discharge end of the drum into the drum forms a combustion chamber. Materials being decontaminated advance through an annular space between the tube and the drum. The tube is axially first of converging and then of diverging shape, as viewed from the discharge end of the drum. A turbo burner injects combustible gases into the tube which are burned within the diverging shape of the tube. A portion of the burned gases reflow from the outlet of tube through the annular space to the discharge end of the drum. In a zone of the drum occupied by the tube materials are heated by conduction and radiation of energy passing through the wall of the tube as well as by convective heating from the reflow gases. Hot gases are exhausted from the drum at the feed end thereof.

Abstract: Material remediation apparatus includes a remediation drum through which materials, such as soil contaminated with hydrocarbons, are advanced from a feed end to a discharge end of the drum. A tube extending concentrically from the discharge end of the drum into the drum forms a combustion chamber. Materials being decontaminated advance through an annular space between the tube and the drum. The tube is axially first of converging and then of diverging shape, as viewed from the discharge end of the drum. A turbo burner injects combustible gases into the tube which are burned within the diverging shape of the tube. A portion of the burned gases reflow from the outlet of tube through the annular space to the discharge end of the drum. In a zone of the drum occupied by the tube materials are heated by conduction and radiation of energy passing through the wall of the tube as well as by convective heating from the reflow gases. Hot gases are exhausted from the drum at the feed end thereof.

Abstract: A burner assembly has a combustion chamber in which combustion takes place in an elongate centrally disposed combustion tube. An outer housing encases the combustion tube and provides an annular space between an inner wall of the housing and the combustion tube. Part of the exhaust gases exiting from the combustion tube are diverted from the downstream end thereof to be returned through the annular space to the upstream end of the combustion tube. Fuel is injected into the diverted exhaust gases, volatilized when in liquid form and mixed with the diverted gases. The fuel and gas mixture is further combined with a buffer gas and becomes entrained into and mixed with a high velocity of combustion air which is injected into the upstream end of the combustion tube. The flame temperature may be monitored and the quantity of the buffer gas added may be controllably varied based on temperature readings from the monitoring process to minimize the generation of nitrous oxides.

Abstract: A gas convection oven having a radiant burner and fuel feeding apparatus which enables the single burner to be operated in either a broil mode or a bake mode. In the broil mode, the radiant burner is operated in conventional manner with the flame being held by an inner screen to heat the outer screen to a radiant luminous temperature. In the bake mode, forced air is injected into the burner by a fan thereby providing a leaner fuel-air mixture with higher velocity. As a result, the flame burns outside the outer screen of the burner with the outer screen serving as a flame holder. Therefore, hot combustion gases as produced while the outer screen remains non-luminous.

Abstract: A high efficiency furnace having a substantially continuous wet heat exchanger wherein such continuous wet operation is provided by raising the dew point of the combustion products by submerged combustion before introduction into said head exchanger. That is, a water holding reservoir is provided between the burner and the heat exchanger, and condensate flows from the heat exchanger back into the reservoir. The combustion products are drawn through the water in the reservoir by providing a partition having a submerged lower portion, and providing a pressure differential between the chambers on the two sides of the partition. The submerged passageway from one chamber to the other may preferably be a serrated bottom edge on the partition or a plurality of apertures in the partition. The pressure differential may be provided by using a combustion blower or alternatively, using an induced draft blower preferably disposed at the flue end of the heat exchanger.

Abstract: A recuperative furnace system for space air and domestic hot water wherein a combustion product heat exchanger and a space air heat exchanger are each operated in counterflow manner. The dew point of the combustion products are elevated before entry into the combustion product heat exchanger and the water to be heated is introduced at the top at a temperature substantially below the natural dew point of the combustion products so that the fins of the heat exchanger are maintained in a substantially continuous wet state by enhanced condensation. The water thus heated is conveyed to a space air heat exchanger in counterflow to the space air so that the space air is heated to a relatively hot temperature (e.g. about 120.degree. F.) while still cooling the water to a low enough temperature (e.g. 90.degree. F.) so that the water can be looped back to the combustion product heat exchanger and still provide continuous wet operation.

Abstract: A washing machine motor having a high resistance rotor to provide high starting torque and low starting current. The permanent split capacitor motor is linked by a speed reducer to the agitator, and a controller alternately reverses the drive direction of the motor to provide the agitator with a relatively high stroke rate such as 60 strokes per minute. In such application, the motor runs cooler than a conventional motor with low rotor resistance because the frequency of starts is high, and, notwithstanding the fact that a high rotor resistance motor is inefficient at running speed, the high rotor resistance motor generates less heat in the critical thermal loading start-up mode.

Abstract: A thermoelectric heat pump attached to a plate evaporator within the freezer compartment. The surface area of the thermoelectric device is maintained at a temperature substantially lower than the temperature of the evaporator plate during the cooling cycle. Accordingly, the majority of frost is collected on the thermoelectric surface area. Defrost is accomplished by reversing the voltage potential across the thermoelectric device and draining the water away in a suitable manner.

Abstract: A forced hot air furnace having a continuously wet recuperative heat exchanger. The recuperative heat exchanger is positioned in the hot air chamber at an upward incline from the firebox to the outside flue. Inclined positioning enables heat exchanger condensate to drain counter to combustion products. Condensate is collected in a reservoir located in the firebox. Combustion products flow over the reservoir thereby becoming elevated in dew point before entering the heat exchanger. Consequently, the amount of condensation formed in the heat exchanger is substantially increased over conventional heat exchangers. Condensate will form along the entire length of the heat exchanger resulting in all wet operation. In another embodiment, continuously wet operation is achieved without a water reservoir. In still another embodiment, the continuously wet recuperative heat exchanger is coupled to the output of a non-recuperative heat exchanger.