The present invention relates to a furnace black having a STSA surface area of at 130 m.sup.2/g to 350 m.sup.2/g wherein the ratio of BET surface area to STSA surface area is less than 1.1 if the STSA surface area is in the range of 130 m.sup.2/g to 150 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.2 if the STSA surface area is greater than 150 m.sup.2/g to 180 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.3 if the STSA surface area is greater than 180 m.sup.2/g, and
the STSA surface area and the BET surface area are measured according to ASTM D 6556 and to a furnace process wherein the stoichiometric ratio of combustible material to O.sub.2 when forming a combustion gas stream is adjusted to obtain a k factor of less than 1.2 and the inert gas concentration in the reactor is increased while limiting the CO.sub.2 amount fed to the reactor. Also provided is an apparatus for conducting the process according to the present invention.

The present invention relates to a device and a method for chemical looping combustion, for which the end of the intake duct (4) opening out within the chamber of the separator (1) is inclined with respect to a horizontal plane (H).

The present invention relates to a furnace black having a STSA surface area of at 130 m.sup.2/g to 350 m.sup.2/g wherein the ratio of BET surface area to STSA surface area is less than 1.1 if the STSA surface area is in the range of 130 m.sup.2/g to 150 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.2 if the STSA surface area is greater than 150 m.sup.2/g to 180 m.sup.2g, the ratio of BET surface area to STSA surface area is less than 1.3 if the STSA surface area i greater than 180 m.sup.2/g; and
the STSA surface area and the BET surface area are measured according to ASTM D 6556 and to a furnace process wherein the stoichiometric ratio of combustible material to O.sub.2 when forming a combustion gas stream is adjusted to obtain a k factor of less than 1.2 and the inert gas concentration in the reactor is increased while limiting the CO.sub.2 amount fed to the reactor. Also provided is an apparatus for conducting the process according to the present invention.

The present invention relates to a furnace black having a STSA surface area of at 130 m.sup.2/g to 350 m.sup.2/g wherein the ratio of BET surface area to STSA surface area is less than 1.1 if the STSA surface area is in the range of 130 m.sup.2/g to 150 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.2 if the STSA surface area is greater than 150 m.sup.2/g to 180 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.3 if the STSA surface area is greater than 180 m.sup.2/g, and
the STSA surface area and the BET surface area are measured according to ASTM D 6556 and to a furnace process wherein the stoichiometric ratio of combustible material to O.sub.2 when forming a combustion gas stream is adjusted to obtain a k factor of less than 1.2 and the inert gas concentration in the reactor is increased while limiting the CO.sub.2 amount fed to the reactor. Also provided is an apparatus for conducting the process according to the present invention.

The present invention relates to a device and a method for chemical looping combustion, for which the end of the intake duct (4) opening out within the chamber of the separator (1) is inclined with respect to a horizontal plane (H).

The present invention relates to a furnace black having a STSA surface area of at 130 m.sup.2/g to 350 m.sup.2/g wherein the ratio of BET surface area to STSA surface area is less than 1.1 if the STSA surface area is in the range of 130 m.sup.2/g to 150 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.2 if the STSA surface area is greater than 150 m.sup.2/g to 180 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.3 if the STSA surface area is greater than 180 m.sup.2/g; and
the STSA surface area and the BET surface area are measured according to ASTM D 6556 and to a furnace process wherein the stoichiometric ratio of combustible material to O.sub.2 when forming a combustion gas stream is adjusted to obtain a k factor of less than 1.2 and the inert gas concentration in the reactor is increased while limiting the CO.sub.2 amount fed to the reactor. Also provided is an apparatus for conducting the process according to the present invention.

A powder discharge system is installed in a circulating water tank for collecting powder generated when an exhaust gas is treated in an exhaust gas treatment apparatus. The powder discharge system includes at least one eductor provided in the circulating water tank. The eductor has a nozzle configured to throttle a flow of water supplied from a pump for pumping water in the circulating water tank, a suction port configured to suck water in the circulating water tank into the eductor by utilizing a reduction of pressure generated when the flow of water is throttled by the nozzle, and a discharge port configured to eject the water sucked from the suction port together with the water discharged from the nozzle toward a bottom of the circulating water tank.

The present invention relates to a furnace black having a STSA surface area of at 130 m.sup.2/g to 350 m.sup.2/g wherein the ratio of BET surface area to STSA surface area is less than 1.1 if the STSA surface area is in the range of 130 m.sup.2/g to 150 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.2 if the STSA surface area is greater than 150 m.sup.2/g to 180 m.sup.2/g, the ratio of BET surface area to STSA surface area is less than 1.3 if the STSA surface area is greater than 180 m.sup.2/g; and
the STSA surface area and the BET surface area are measured according to ASTM D 6556 and to a furnace process wherein the stoichiometric ratio of combustible material to O.sub.2 when forming a combustion gas stream is adjusted to obtain a k factor of less than 1.2 and the inert gas concentration in the reactor is increased while limiting the CO.sub.2 amount fed to the reactor. Also provided is an apparatus for conducting the process according to the present invention.

The present technology describes various embodiments of systems and methods for handling emissions. More specifically, some embodiments are directed to systems and methods for collecting heated particulate from a coal processing system. In one embodiment, a method of handling emissions from a coal processing system includes inletting the emissions into a duct. The emissions include heated particulate. The method further includes slowing a speed of the emissions traveling through the duct and disengaging the heated particulate from the emissions without the use of a physical barrier. In some embodiments, the heated particulate is slowed, cooled, and diverted from an emissions pathway into a collection bin.

An apparatus for reducing air pollution includes a piping system, at least one compressor fan, a cooling system, and a tank having at least one first filter and at least one second filter separated by at least one intermediary member. The piping system is coupled to a cooling system adapted to saturate the exhaust with water. The exhaust and contaminated water flow downward into the tank containing at least one first filter and at least one second filter separated by at least one intermediary member where the exhaust and the contaminated water are filtered. The cleaned water is recirculated through the cooling system, and the exhaust is filtered a second time through the at least one second filter, the at least one intermediary member, and the at least one first filter prior to release into the atmosphere. A method for reducing air pollution from exhaust is also provided.