The present invention relates to a denitration and waste heat recovery integrated furnace, comprising a denitration system, a desulfurization system and a waste heat recovery system. An air outlet of the denitration system is connected to an inlet of a dust collector (4), an outlet of the dust collector (4) is connected to an air inlet of the desulfurization system, an air outlet of the desulfurization system is connected to an air compressor (6) of the waste heat recovery system, and the waste heat recovered by the air compressor (6) is used for heat energy utilization of other departments.

In one aspect, structural catalyst bodies comprising one or more gradients of catalytic material are provided herein. In some embodiments, a structural catalyst body described herein comprises an inner partition wall having a first surface and a second surface opposite the first surface, the inner partition wall having a gradient of catalytic material along the width of the inner partition wall.

A gas turbine system may include an exhaust gas processing system configured to process exhaust gas received from a gas turbine engine of the system. An exhaust path of the exhaust processing system is configured to flow the exhaust gas through the exhaust processing system. A tempering air system of the exhaust processing system is configured to introduce tempering air into the exhaust path to cool the exhaust gas. The tempering air system includes a tempering air pathway extending from an air inlet of the tempering air system to a tempering air outlet where tempering air is introduced from the tempering air system and into the exhaust path. A filter system of the tempering air system has a hydrophobic filter positioned along the tempering air pathway, the hydrophobic filter being configured to remove hygroscopic and deliquescent materials from the air flowing through the tempering air pathway.

This desulfurization device is for desulfurizing a discharge gas which contains sulfur oxides and which was discharged from a device for sulfuric acid production that includes a concentrated-sulfuric-acid production step in which sulfur trioxide gas obtained by oxidizing sulfur dioxide gas is absorbed in an aqueous sulfuric acid solution while supplying water thereto to thereby produce sulfuric acid having a concentration as high as 90 wt % or more but less than 99 wt %, the desulfurization device comprising: a desulfurization tower in which the sulfur oxides are removed from the discharge gas and, simultaneously therewith, dilute sulfuric acid is formed from the sulfur oxides; and a dilute sulfuric acid mixer which, in the concentrated-sulfuric-acid production step, mixes the dilute sulfuric acid with the aqueous sulfuric acid solution.

The present invention relates to a denitration and waste heat recovery integrated furnace, comprising a denitration system, a desulfurization system and a waste heat recovery system. An air outlet of the denitration system is connected to an inlet of a dust collector (4), an outlet of the dust collector (4) is connected to an air inlet of the desulfurization system, an air outlet of the desulfurization system is connected to an air compressor (6) of the waste heat recovery system, and the waste heat recovered by the air compressor (6) is used for heat energy utilization of other departments.

The description relates to a process for reducing acid plume from stacks from coal-fired combustors operating at varying loads, which have typically been treated by back-end calcium carbonate (limestone) which has not been able to effectively control visible acid plume as power is ramped up from low load. According to the process, as high sulfur and high iron coals are burned in a combustor, magnesium hydroxide slurry is introduced into hot combustion gases in or near the combustion zone. And, during ramp up to high load from a period of operation at low load, additional magnesium hydroxide is introduced into an intermediate-temperature zone.

A system for reducing SO.sub.2 emissions comprises a hydrogenation reactor, a tail gas cooler, a contact condenser, a hydrolysis reactor, and an absorber. The hydrogenation reactor is configured to receive a Claus tail gas and convert at least a portion of SO.sub.2 in the Claus tail gas to H.sub.2S to produce a hydrogenated Claus tail gas stream. The hydrolysis reactor is configured to convert at least a portion of COS to H.sub.2S. The absorber comprises an amine-based solvent and is configured to absorb at least a portion of the H.sub.2S and recycle the H.sub.2S to the Claus plant.

A gas processing apparatus of an embodiment has stacks, gas flow paths, an AC power supply, and a flow limiter. The stacks are away from each other and in parallel. Each stack includes a dielectric substrate and a first to a third electrode. The first and second electrodes are respectively disposed on the first and second main surfaces of the dielectric substrate. The third electrode is disposed inside the dielectric substrates. The gas flow paths supply a target gas between the stacks, The AC power supply applies an AC voltage across the first and second electrodes and the third electrodes, so as to generate plasma induced flows of the target gas between the dielectric substrates. The flow limiter is disposed on a downstream side of the stacks and limits a flow rate of the target gas.

There is provided a process for converting a CO.sub.2 and/or H.sub.2O-containing gas mixture, such as flue gas, into a low-carbon fuel. The process comprises contacting the gas mixture with a catalyst comprising: a catalyst body having metallic iron exposed superficially and pores. There is also provided processes for manufacturing an iron-based porous catalyst as porous monoliths having exposed catalytically active surfaces. There is also provided an iron-based catalyst, including iron oxides, to at least partially remove SO.sub.x from a gas mixture and a process for at least partially removing SO.sub.x from a gas mixture using the iron-based catalyst.

The present invention discloses a preparation method for an activated coke catalyst capable of simultaneously removing NO, SO.sub.2, and HCl. The method includes: step 1: crushing and sieving activated coke to obtain coke particles with a particle size of 40-60 microns; step 2: putting the activated coke in an oxidizing agent, stirring at 80 C. for 8 h to allow for a thorough mixing and reaction, washing the activated coke obtained after the reaction until a neutral pH is reached, and drying to obtain activated coke with oxygen-containing functional groups; and step 3: impregnating, by equivalent-volume impregnation, the activated coke with oxygen-containing functional groups obtained in step 2 with a copper nitrate trihydrate aqueous solution for 24 h, drying, and putting the activated coke in a resistance furnace, and introducing argon for calcination to obtain the activated coke catalyst capable of simultaneously removing NO, SO.sub.2, and HCl.