A process and a device for treating a flow of furnace gas with a pressure of more than 1 bar flowing through a channel. A powder agent, such as a powder comprising alkali reagents, such as lime, and/or absorbents, such as activated coal, is injected under an overpressure into the furnace gas flow via an injector which is positioned centrally within the channel. The powder agent may be fluidized. The pressure for injecting the powder may be adjusted by controlling the volume of fluidization gas vented via a venting outlet.

Systems and methods for reducing the capital and operating costs of a smelting process system and improving the environmental impact of the smelting process using an IGT system to remove and filter undesirable and environmentally hazardous gases and particulates from each electrolytic cell in the smelting process system.

Systems and methods for reducing the capital and operating costs of a smelting process system and improving the environmental impact of the smelting process using an IGT system to remove and filter undesirable and environmentally hazardous gases and particulates from each electrolytic cell in the smelting process system.

Embodiments relate to systems and methods for fluidization in industrial hygiene applications. The method includes collecting air samples of contaminants onto the surface of fluidized activated carbon particulate as opposed to fixed-bed particulate. The adsorbates include toluene (a cyclic compound) and n-hexane (an open-chain compound). The obtained results are analyzed and discussed in terms of breakthrough times. The input parameters are the initial concentration of toluene or n-hexane in the air feed stream and the amount of the sorbent used. The feed flow rate is at 2 liters/min, and the temperature and humidity are kept constant at their prevailing laboratory conditions, i.e., 222 C. and 342% RH, respectively.

Embodiments relate to systems and methods for fluidization in industrial hygiene applications. The method includes collecting air samples of contaminants onto the surface of fluidized activated carbon particulate as opposed to fixed-bed particulate. The adsorbates include toluene (a cyclic compound) and n-hexane (an open-chain compound). The obtained results are analyzed and discussed in terms of breakthrough times. The input parameters are the initial concentration of toluene or n-hexane in the air feed stream and the amount of the sorbent used. The feed flow rate is at 2 liters/min, and the temperature and humidity are kept constant at their prevailing laboratory conditions, i.e., 222 C. and 342% RH, respectively.

A carbon capture device comprising a flue gas input, a flue gas output, a carbon adsorption zone that is in fluid communication with the flue gas input and in fluid communication with the flue gas output, where a first flue gas communication channel comprises the carbon adsorption zone, where the first flue gas communication channel comprises a first fluid input and a first fluid output, and the carbon adsorption zone comprises a first CO.sub.2 sorbent material positioned downstream from the first fluid input and upstream to/of the first fluid output, where the first fluid input is in fluid communication with the flue gas input, and where the flue gas is directed past the CO.sub.2 sorbent material and towards the first fluid output, where the first fluid output is in fluid communication with the flue gas output, a carbon desorption zone, where the carbon desorption zone comprises a second CO.sub.2 sorbent material, and an actuation device where the actuation device is configured to transport carbon-rich first CO.sub.2 sorbent material from the carbon adsorption zone to the carbon desorption zone and to transport carbon-lean second CO.sub.2 sorbent material from the carbon desorption zone to the carbon adsorption zone.

A carbon capture device comprising a flue gas input, a flue gas output, a carbon adsorption zone that is in fluid communication with the flue gas input and in fluid communication with the flue gas output, where a first flue gas communication channel comprises the carbon adsorption zone, where the first flue gas communication channel comprises a first fluid input and a first fluid output, and the carbon adsorption zone comprises a first CO.sub.2 sorbent material positioned downstream from the first fluid input and upstream to/of the first fluid output, where the first fluid input is in fluid communication with the flue gas input, and where the flue gas is directed past the CO.sub.2 sorbent material and towards the first fluid output, where the first fluid output is in fluid communication with the flue gas output, a carbon desorption zone, where the carbon desorption zone comprises a second CO.sub.2 sorbent material, and an actuation device where the actuation device is configured to transport carbon-rich first CO.sub.2 sorbent material from the carbon adsorption zone to the carbon desorption zone and to transport carbon-lean second CO.sub.2 sorbent material from the carbon desorption zone to the carbon adsorption zone.

An emissions control system including a fluidized bed apparatus containing a reactive sorbent material is disclosed for gaseous and non-gaseous contaminated emissions. The reactive sorbent material may be CZTS, CZTS-Alloy, or a carbon-based sorbent material. The fluidized bed apparatus is configured with one or more closed loop sorbent recycling subsystems. The sorbent recycling subsystems include the capability to separate sorbents from each other, separate contaminates from sorbents for disposal and/or recycling, clean and/or rejuvenate sorbents for return to the fluidized bed apparatus, dispose of spent and exhausted sorbents, and replace the spent and exhausted sorbents with new sorbent to maintain consistent sorbent function in the fluidized bed apparatus. Monitoring sensors provide information useful in a method for establishing and maintaining consistent process parameter controls.

An emissions control system including a fluidized bed apparatus containing a reactive sorbent material is disclosed for gaseous and non-gaseous contaminated emissions. The reactive sorbent material may be CZTS, CZTS-Alloy, or a carbon-based sorbent material. The fluidized bed apparatus is configured with one or more closed loop sorbent recycling subsystems. The sorbent recycling subsystems include the capability to separate sorbents from each other, separate contaminates from sorbents for disposal and/or recycling, clean and/or rejuvenate sorbents for return to the fluidized bed apparatus, dispose of spent and exhausted sorbents, and replace the spent and exhausted sorbents with new sorbent to maintain consistent sorbent function in the fluidized bed apparatus. Monitoring sensors provide information useful in a method for establishing and maintaining consistent process parameter controls.

Provided is a renewable wet desulfurization process using a suspension bed, comprising mixing the desulfurization slurry with a hydrogen sulfide containing gas to obtain a first mixture, and passing the first mixture into a suspension bed reactor from bottom to top, with controlling the first mixture to have a dwell time of 5-60 minutes in the suspension bed reactor to allow they contact and react sufficiently with each other; and subjecting a second mixture obtained from the reaction to gas liquid separation to produce a rich solution and a purified gas, subjecting the resulting rich solution to flash evaporation and then reacting with an oxygen-containing gas for carrying out regeneration. The process of the present invention may reduce the hydrogen sulfide content in the hydrogen sulfide containing gas from 2.4-140 g/Nm.sup.3 to 50 ppm or less, so that the desulfurization efficiency is 98% or more. The present invention can achieve regeneration of a spent desulfurizer with a regeneration efficiency as high as 65%-83%, and the barren solution obtained by the regeneration may be recycled for being used as the desulfurization slurry, without generating secondary pollution, which is very suitable for industrial promotion.