Process for reducing fossil co2 emissions

Patent metadata

Field	Value
Publication number	US-2025229224-A1
Application number	US-202318852630-A
Country	US
Kind code	A1
Filing date	Mar 29, 2023
Priority date	Mar 29, 2022
Publication date	Jul 17, 2025
Grant date	—

Abstract

A process for operating an oxidizable combustion gas cleaning unit in a metallurgical plant, including the steps of: (a) passing an oxidizable combustion gas from a metallurgical reactor, in particular a blast furnace gas from a blast furnace, in a packed bed scrubber arrangement through a packed bed in countercurrent with a washing water or in a spray scrubber arrangement to remove cyanide compounds, in particular hydrogen cyanide, and to increase the removal of chloride compounds, in particular hydrogen chloride, from the combustion gas by solubilizing the cyanide and chloride compounds in the washing water, (b) collecting the washing water containing solubilized cyanide and chloride compounds at a bottom end of the packed bed or spray scrubber arrangement, and (c) collecting a cleaned oxidizable combustion gas at a top of the packed bed or spray scrubber arrangement, wherein a base is added to the washing water before step (a).

First claim

1 . A process for operating an oxidizable combustion gas cleaning unit in a metallurgical plant, comprising the steps of:
(a) passing an oxidizable combustion gas from a blast furnace gas from a blast furnace in a packed bed scrubber arrangement through a packed bed in countercurrent with a washing water or in a spray scrubber arrangement to remove cyanide compounds and to increase the removal of chloride compounds from said combustion gas by solubilizing said cyanide and chloride compounds in said washing water, (b) collecting the washing water containing solubilized cyanide and chloride compounds at a bottom end of the packed bed or spray scrubber arrangement, and (c) collecting a cleaned oxidizable combustion gas at a top of the packed bed or spray scrubber arrangement,
wherein a base is added to the washing water before step (a), said base being NaOH, which is added between 3.5% and 6.5% above the stoichiometric amount with respect to the cyanide and chloride compounds to be removed from the oxidizable combustion gas.

2 . The process as claimed in claim 1 , wherein the packed bed scrubber arrangement comprises, a column comprising a random packed bed unit, optionally comprising a plurality of packed bed zones separated by redistribution zones, the packed bed unit being supported by at least one perforated support plate, a washing water spray distributor arranged above said packed bed for distributing the washing water into the packed bed unit, a washing water collecting unit arranged at the bottom end of the packed bed scrubber arrangement below the packed bed, said washing water collecting unit comprising a duct for draining the washing water containing cyanide compounds from the packed scrubber arrangement, a gas feeding unit arranged for feeding the oxidizable combustion gas into the chamber below the packed bed unit, and a cleaned oxidizable combustion gas discharge unit on a top of the packed bed column comprising a duct for discharging the cleaned oxidizable combustion gas and placed after a mist eliminator.

3 . The process as claimed in claim 1 , wherein the washing water to oxidizable combustion gas ratio in the packed bed in step (a) is between 3.5 and 6.5 L/Nm 3 .

4 . The process as claimed in claim 1 , wherein the mean residence time of the combustion gas in the packed bed in step (a) is between 3.4 and 5.8 s.

5 . The process as claimed in claim 1 , wherein the packed bed has a total (wet) contact surface, comprising the total surface of the (wet) packed bed can be in contact with the oxidizable combustion gas, between 0.09 and 0.15 m 2 /(Nm 3 /h).

6 . The process as claimed in claim 1 , wherein the packed bed scrubber arrangement is operated at near atmospheric pressure.

7 . The process as claimed in claim 1 , wherein the temperature inside the packed bed is between ambient temperature and 70° C.

8 . The process as claimed in claim 1 , wherein the spray scrubber arrangement comprises a column comprising a spray section unit comprising at least four independent spray stages distributed along a height of the column and composed of a set of nozzle units located on multiple ramps and distributing of the washing water in the form of droplets, wherein the oxidizable combustion gas is fed through a gas feeding unit into the column below the spray section unit, wherein the washing water is collected in a washing water collecting unit arranged at a bottom end of the spray scrubber arrangement below the spray section unit and the gas feeding unit, said washing water reservoir unit comprising a duct for draining the washing water containing cyanide and chloride compounds from the spray scrubber arrangement, and wherein the cleaned oxidizable combustion gas is passed through a mist eliminator before being discharged in an oxidizable combustion gas discharge unit on a top of the spray column comprising a duct for discharging the cleaned oxidizable combustion gas.

9 . The process as claimed in claim 1 , wherein the flow of oxidizable combustion gas within the spray scrubber arrangement is regulated by deviating part of the flow of oxidizable combustion gas through a by-pass external to the column unit.

10 . The process as claimed in claim 8 , wherein the global ratio of washing water distributed in the different spray stages to oxidizable combustion gas in step (a) is between 0.8 and 2.9 L/Nm 3 , depending on the amount of cyanide and chloride compounds to be removed and on the desired removal and in order to manage the concentration of cyanides and chloride compounds in the washing water.

11 . The process as claimed in claim 8 , wherein a mean residence time of the oxidizable combustion gas in the spray section unit in step (a) is between 2 and 8 s.

12 . The process as claimed in claim 8 , wherein the nozzles of the spray scrubber arrangements are axial flow full cone nozzles providing droplets having a Sauter mean diameter between 1100 and 1150 μm through a proper setup of the nozzle pressure.

13 . The process as claimed in claim 8 , wherein the spray scrubber arrangement is operated at near atmospheric pressure.

14 . The process as claimed in claim 8 , wherein the temperature inside the spray column is below the water boiling temperature, between ambient temperature and 70° C.

15 . The process as claimed in claim 1 , comprising the further step of:
(d) feeding the washing water from step (b) to a dust abatement unit to reduce dust contents of the oxidizable combustion gas upstream of the scrubber arrangement in step (a), (e) collecting dust abatement water from step (d) containing the dust abated in the dust abatement unit.

16 . The process as claimed in claim 15 , wherein a base is added to the washing water before step (d), said base being chosen among oxides and hydroxides of alkali metals and alkaline earth metals comprising NaOH, KOH, Ca(OH) 2 or mixtures thereof.

17 . The process as claimed in claim 15 , further comprising the step (f) of treating the washing water from step (b) to remove cyanide compounds, in particular free cyanides, and/or the step (g) for further removing residual cyanide from the blowdown of the cleaning process of dust abatement water from step (e).

18 . The process as claimed in claim 1 , further comprising an oxidation step for cyanide removal from washing water based on the use of H 2 O 2 and a Cu catalyst, carried out in two continuously mixed reactor arrangements in series, wherein each reactor arrangement comprises a vertical tank including, an impeller unit, an impeller engine unit, a baffle unit for agitation and for preventing formation of a vortex, a duct for feeding washing water to a washing water feeding unit, placed near to the top of the vertical tank unit, a duct placed at the bottom of the vertical tank unit for draining the treated washing water, said washing water outlet unit, and reagents and catalyst feeding units placed at the top of the reactor arrangement.

19 . The process as claimed in claim 18 , wherein a residence time of the washing water in the continuously mixed reactor arrangements is between 40 and 65 minutes for the first reactor arrangement and 45 and 85 minutes for the second reactor arrangement.

20 . The process as claimed in claim 18 , wherein H 2 O 2 dosage is comprised between 0.35-0.55 g of H 2 O 2 (30% wt.) per liter of washing water.

21 . The process as claimed in claim 18 , wherein Cu-based catalyst is dosed in order to have a concentration of 40 mg/L of Cu 2+ in the washing water.

Assignees

• Wurth Paul Sa

Inventors

• Spadoni Luca
• Micheletti Lorenzo
• Olcese Alessandro
• Fossati Davide
• Veneziano Francesco
• Matino Ismael
• Zaccara Antonella
• Petrucciani Alice
• Colla Valentina
• Branca Teresa Annunziata

Classifications

• C21B7/002 Primary

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• B01F2215/0481

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• B01F2215/0477

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• B01F2215/0422

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• B01D2258/0283

  Flue gases · CPC title