DE-102024132889-A1 - Method for the industrial production of an alkaline earth metal compound other than an alkaline earth metal sulfate, corresponding production plant, corresponding uses, corresponding kit and corresponding use of a kit

Abstract

A process for the industrial production of an alkaline earth metal compound other than an alkaline earth metal sulfate, comprising at least the following steps: S1) (i) Manufacture or supply of an alkaline earth metal sulfate and separately (ii) Production or supply of a reducing gas; S2) Reducing the alkaline earth metal sulfate produced or provided in step S1) using the reducing gas so that a corresponding alkaline earth metal sulfide results.

Inventors

• Ferdinand Hardinghaus
• Achim ENGELS
• Uwe Lazer
• Erik BONMANN
• Erik Reichelt
• Michael Gallwitz
• Gregor Herz
• Sebastian Hilbig

Assignees

• Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung eingetragener Verein
• Kandelium Barium Strontium GmbH & Co. KG

Dates

Publication Date

20260513

Application Date

20241111

Claims (18)

1. A process for the industrial production of an alkaline earth metal compound other than an alkaline earth metal sulfate, comprising at least the following steps: S1) (i) Production or provision of an alkaline earth alkaline earth metal sulfates and separately (ii) producing or providing a reducing gas; S2) reducing the alkaline earth metal sulfate produced or provided in step S1) by means of the reducing gas so that a corresponding alkaline earth metal sulfide results.
2. Procedure according to the preceding Claim 1 , wherein the alkaline earth metal compound that is not an alkaline earth metal sulfate is selected from the group consisting of: - barium carbonate, - barium soaps, - barium sulfonates, - barium titanate ( BaTiO3 ), - barium ferrite ( BaFe12O19 ), - barium chlorate (Ba( CO3 ) 2 ) , - barium chloride ( BaCl2 ), - lithopones ( BaSO4 ·ZnS), - barium hydroxide (Ba(OH) 2 ), - barium oxide ( BaO ), - barium oxalate ( BaC2O4 ), - barium acetate (Ba( C2H3O2 ) 2 ) , - barium chromate ( BaCrO4 ), - other barium compounds, - strontium carbonate, - strontium soaps , - strontium sulfonates, - strontium titanate ( SrTiO3 ), - strontium ferrite ( SrFe12O ) 19 ), - Strontium chlorate (Sr(ClO 3 ) 2 ), - Strontium chloride (SrCl 2 ), - Strontium hydroxide (Sr(OH) 2 ), - Strontium oxide (SrO ), - Strontium oxalate (SrC 2 O 4 ), - Strontium acetate (Sr(C 2 H 3 O 2 ) 2 ), - Strontium chromate (SrCrO 4 ), and - other strontium compounds.
3. Procedure according to the preceding Claim 1 , with the following additional step: - with the following additional step: S3) Preparation of an aqueous solution comprising dissolved components of the alkaline earth metal sulfide resulting in step S2), such that an aqueous solution comprising a dissolved alkaline earth metal sulfide results; and/or - with the following additional step: S4) Introduction of gaseous carbon dioxide into the aqueous solution comprising a dissolved alkaline earth metal sulfide resulting in step S3), - such that an alkaline earth metal carbonate results and precipitates wholly or partially as a solid; and - such that hydrogen sulfide ( H2S ) results.
4. A method according to any one of the preceding claims, wherein - the alkaline earth metal sulfate produced or provided in step S1) is selected from the group consisting of: - barium sulfate and - strontium sulfate; and/or - wherein the reducing gas used in step S2) for the reduction of the alkaline earth metal sulfate is selected from the group consisting of: - hydrogen ( H2 ), - ammonia ( NH3 ), - methane ( CH4 ) and - mixtures thereof; and/or - the alkaline earth metal sulfide resulting in step S2) is selected from the group consisting of: - barium sulfide and - strontium sulfide; and/or - the alkaline earth metal carbonate resulting in step S4) is selected from the group consisting of: - barium carbonate ( BaCO3 ) and - strontium carbonate ( SrCO3 ).
5. A method according to any one of the preceding claims – with the following additional step: S5) separating at least a portion of the alkaline earth metal carbonate precipitated as a solid in step S4), such that a separated alkaline earth metal carbonate results, wherein the separation preferably comprises centrifugation and/or filtration, preferably centrifugation; and optionally with the following additional step: S6) drying at least a portion of the separated alkaline earth metal carbonate resulting in step S5), such that a dried alkaline earth metal carbonate results; and/or – with the following additional step: S7) calcining – the separated alkaline earth metal carbonate resulting in step S5) and/or – the dried alkaline earth metal carbonate resulting in step S6), such that a calcined alkaline earth metal carbonate results; and/or - with the following additional step between the preparation or provision in step S1) and the reduction in step S2): S1a) Heating the alkaline earth metal sulfate prepared or provided in step S1), preferably heating to a temperature in the range of 400 °C to 1400 °C, preferably to a temperature in the range of 500 °C to 1300 °C, particularly preferably to a temperature in the range of 600 °C to 1100 °C, most preferably to a temperature in the range of 700 °C to 950 °C; and/or - with the following additional step between the preparation or provision in step S1) and the Reducing in step S2): S1b) of the reducing gas produced or provided in step S1), preferably heating to a temperature in the range of 400 °C to 1400 °C, preferably to a temperature in the range of 500 °C to 1300 °C, particularly preferably to a temperature in the range of 600 °C to 1100 °C, most preferably to a temperature in the range of 700 °C to 950 °C.
6. A process according to any one of the preceding claims, wherein step S2) of the process is carried out as a continuous process; or step S2) of the process is carried out as a batch process; and/or wherein the alkaline earth metal carbonate precipitated as a solid in step S4); and/or the separated alkaline earth metal carbonate resulting in step S5); and/or the dried alkaline earth metal carbonate resulting in step S6); is selected from the group consisting of: barium carbonate ( BaCO3 ), preferably barium carbonate comprising less than 10 wt.% impurities, preferably less than 7 wt.%, particularly preferably less than 5 wt.%, most preferably less than 2 wt.%, in each case based on the total mass of barium carbonate and the included impurities; and/or - less than 2 wt.% strontium oxide (SrO), preferably less than 1.8 wt.%, particularly preferably less than 1.6 wt.%, most preferably less than 1.45 wt.%, in each case based on the total mass of barium carbonate and the included minor components; and - strontium carbonate ( SrCO₃ ), preferably comprising - less than 10 wt.% minor components, preferably less than 7 wt.%, particularly preferably less than 5 wt.%, most preferably less than 2 wt.%, in each case based on the total mass of strontium carbonate and the included minor components; and/or - less than 2 wt.% barium oxide (BaO), preferably less than 1.8 wt.%, particularly preferably less than 1.6 wt.%, most preferably less than 1.45 wt.%, in each case based on the total mass of strontium carbonate and the included minor components; and/or - wherein the hydrogen sulfide resulting in step S4) is separated from the gas phase and/or - is further processed to sulfur dioxide and elemental sulfur; preferably in a Claus process; and/or - is further processed to NaHS; and/or - is used in a chemical process that does not have elemental sulfur as the target product and does not have NaHS as the target product.
7. A method according to any one of the preceding claims, wherein step S2) of the method is carried out wholly or partly, preferably wholly, in a rotary kiln, and wherein the alkaline earth metal sulfate has a temperature in the range of 400 °C to 1400 °C when produced or provided in step S1), preferably a temperature in the range of 500 °C to 1300 °C, particularly preferably a temperature in the range of 600 °C to 1100 °C, and most preferably a temperature in the range of 700 °C to 950 °C; and/or wherein the reducing gas has a temperature in the range of 400 °C to 1400 °C when produced or provided in step S1), preferably a temperature in the range of 500 °C to 1300 °C, particularly preferably a temperature in the range of 600 °C to 1100 °C, and most preferably a temperature in the range of 700 °C to 1050 °C; and/or - wherein the temperature during the process is in the range of 400 °C to 1400 °C, preferably in the range of 500 °C to 1200 °C, particularly preferably in the range of 600 °C to 1000 °C, and most preferably in the range of 700 °C to 950 °C; and/or - wherein step S2) is carried out at a pressure in the range of 0.5 bar to 1.5 bar, preferably at a pressure in the range of 0.7 bar to 1.3 bar, particularly preferably at a pressure in the range of 0.8 bar to 1.2 bar, most preferably at a pressure in the range of 0.85 bar to 1.1 bar, and preferably at a pressure in the range of 0.9 bar to 0.99 bar; and/or - wherein in step S2) solids and reducing gas pass through the rotary kiln in countercurrent flow; and/or - wherein, for heating the shaft furnace, reducing gas, preferably methane gas, is preheated to a temperature in the range of 500°C to 1300°C, preferably in the range of 600°C to 1100°C, particularly preferably in the range of 700°C to 1050°C in a preheater, preferably an electric preheater, before entering the shaft furnace; and/or - wherein oxygen is additionally supplied to the rotary kiln to heat it, so that a portion of the reducing gas introduced into the shaft kiln reacts in an exothermic reaction with oxygen in the shaft kiln; and/or - wherein the rotary kiln is electrically heated; and/or - wherein the gas mixture exiting the rotary kiln has a higher temperature than the solids entering the rotary kiln; and/or - wherein the gas mixture exiting the rotary kiln is wholly or partially processed after exiting the rotary kiln, resulting in a processed gas mixture, and wherein preferably - the processing includes the removal of particulate substances; and/or - the processing includes the removal of water; and/or - the processing includes the removal of carbon dioxide ( CO2 ); and/or - portions of the processed gas mixture are fed into the process as part of the reducing gas; and/or - the particulate substances separated during the separation of particulate substances are fed into the process as part of the alkaline earth metal sulfate; and/or - wherein the gas mixture exiting the rotary kiln is used wholly or partly for heat recovery after exiting the rotary kiln.
8. A method according to any of the preceding claims, wherein step S2) of the method is carried out wholly or partly, preferably wholly, in a shaft furnace, and wherein the alkaline earth metal sulfate has a temperature in the range of 400 °C to 1400 °C when produced or provided in step S1), preferably a temperature in the range of 500 °C to 1300 °C, particularly preferably a temperature in the range of 600 °C to 1100 °C, most preferably a temperature in the range of 700 °C to 950 °C; and/or - wherein the reducing gas, when produced or provided in step S1), has a temperature in the range of 400 °C to 1400 °C, preferably a temperature in the range of 500 °C to 1300 °C, particularly preferably a temperature in the range of 600 °C to 1100 °C, and most preferably a temperature in the range of 700 °C to 1050 °C; and/or - wherein step S2) is carried out at a pressure of 0.8 bar to 15 bar, preferably at a pressure of 3 bar to 10 bar, particularly preferably at a pressure of 4 bar to 8.5 bar, and most preferably at a pressure of 6.5 bar to 7.8 bar; and/or - wherein the height of the solid bed in the shaft furnace is in the range of 1 m to 30 m, preferably in the range of 2 m to 20 m, particularly preferably in the range of 6 to 15 m, and most preferably in the range of 8 m to 12 m; and/or - wherein in step S2) during reduction the bulk density of the solid in the shaft furnace is in the range of 0.6 t/ m³ to 3.2 t/ m³ , preferably in the range of 0.9 t/ m³ to 2.9 t/ m³ , particularly preferably in the range of 1.3 t/ m³ to 2.7 t/ m³ , and most preferably in the range of 1.5 kg/ m³ to 2.6 kg/ m³ , in each case based on the average bulk density of the entire solid bed; and/or - wherein the temperature during the process is in the range of 400 °C to 1400 °C, preferably in the range of 500 °C to 1200 °C, particularly preferably in the range of 600 °C to 1000 °C, and most preferably in the range of 700 °C to 950 °C; and/or - wherein the alkaline earth metal sulfide resulting in step S2) leaves the shaft furnace at a temperature of less than 410 °C, preferably less than 400 °C, particularly preferably less than 390 °C, and most preferably less than 385 °C; and/or - wherein in step S2) solids and reducing gas pass through the shaft furnace in countercurrent flow; and/or - wherein in step S2) the solids transport is gravity-driven; and/or - wherein reducing gas at a temperature of less than 40 °C, preferably less than 35 °C, particularly preferably less than 30 °C, and most preferably less than 25 °C, is introduced into the shaft furnace for cooling; and/or - wherein reducing gas, preferably methane gas, is preheated to a temperature in the range of 500 °C to 1300 °C, preferably 600 °C to 1100 °C, particularly preferably 700 °C to 1050 °C, in a preheater, preferably an electric preheater, before entering the shaft furnace for heating; and/or - wherein oxygen is additionally supplied to the shaft furnace for heating, so that a portion of the gas entering the shaft pipe... the reduction gas introduced into the shaft tube furnace reacts in an exothermic reaction with oxygen; and/or - wherein the shaft furnace is electrically heated; and/or - wherein the gas mixture exiting the shaft furnace has a higher temperature than the solids entering the shaft furnace; and/or - wherein the gas mixture exiting the shaft furnace is wholly or partially processed after exiting the shaft furnace, resulting in a processed gas mixture, and wherein preferably - the processing includes the removal of particulate substances; and/or - the processing includes the removal of water; and/or - the processing includes the removal of carbon dioxide ( CO₂ ); and/or - portions of the processed gas mixture are fed into the process as part of the reduction gas; and/or - the particulate substances separated during the removal of particulate substances are fed into the process as part of the alkaline earth metal sulfate; and/or - wherein the gas mixture exiting the shaft furnace is used wholly or partially for heat recovery after exiting the shaft furnace.
9. A method according to any one of the preceding claims, - wherein celestine is provided wholly or partially as the alkaline earth metal sulfate in step S1); or - wherein barite is provided wholly or partially as the alkaline earth metal sulfate in step S1); and/or - wherein the alkaline earth metal sulfate is produced or provided in step S1 as a bulk material, preferably as a powdered bulk material and/or as a granulated bulk material.
10. Production plant for the manufacture of an alkaline earth metal compound other than an alkaline earth metal sulfate, preferably an alkaline earth metal carbonate, and particularly preferably an alkaline earth metal carbonate selected from the group consisting of barium carbonate and strontium carbonate, wherein the production plant comprises at least: A) a device for producing or providing a reducing gas, preferably a reducing gas selected from the group consisting of methane, hydrogen, and ammonia; B) a device for producing or providing an alkaline earth metal sulfate, preferably an alkaline earth metal sulfate selected from the group consisting of barium sulfate and strontium sulfate; C) a reactor for the reduction of an alkaline earth metal sulfate using a reducing gas.
11. Production plant according to Claim 10 , further comprising D) a container for an aqueous solution comprising a dissolved alkaline earth metal sulfide, wherein the container is preferably connected to a device for supplying water; and/or E) a stirring device for an aqueous solution comprising a dissolved alkaline earth metal sulfide; and/or F) a device for introducing carbon dioxide into a container for an aqueous solution comprising a dissolved alkaline earth metal sulfide; and/or G) a device for separating hydrogen sulfide, preferably a device for separating hydrogen sulfide comprising one or more containers in which the suspension containing the alkaline earth metal carbonate is passed through with gaseous carbon dioxide; and/or H) a device for separating solids, preferably alkaline earth metal carbonates, particularly preferably alkaline earth metal carbonates selected from the group consisting of barium carbonate and strontium carbonate, from an aqueous solution; wherein the device is preferably selected from the group consisting of a centrifugation apparatus and a filtration apparatus; The apparatus is particularly preferably a centrifugation apparatus; and/or I) an apparatus for drying solid alkaline earth metal carbonates; and/or J) an apparatus for calcining alkaline earth metal carbonates; and/or K) an apparatus for heating the reactor for the reduction of an alkaline earth metal sulfate by means of a reducing gas; and/or L) an apparatus for heating an alkaline earth metal sulfate, preferably an alkaline earth metal sulfate selected from the group consisting of barium sulfate and strontium sulfate, to temperatures in the range of 400 °C to 1400 °C, preferably to temperatures in the range of 500 °C to 1300 °C, particularly preferably to a temperature in the range of 600 °C to 1100 °C, most especially preferably to a temperature in the range of 700 °C to 950 °C; and/or M) a device for heating a reducing gas, in particular methane and/or hydrogen, preferably to a temperature in the range of 400 °C to 1400 °C, particularly preferably to a temperature in the range of 700 °C to 1300 °C, most preferably to a temperature in the range of 750 °C to 1200 °C, very particularly preferably to a temperature in the range of 800 °C to 1050 °C; and/or N) a device for drying an alkaline earth metal sulfate, preferably an alkaline earth metal sulfate selected from the group consisting of: barium sulfate and strontium sulfate.
12. Production plant according to one of the preceding Claims 10 or 11 , - wherein the reactor C) for the reduction of an alkaline earth metal sulfate is selected from the group of reactors comprising - shaft furnace and - rotary kiln; and/or - wherein the reactor C) for the reduction of an alkaline earth metal sulfate is sealed in such a way that there are no unacceptable leaks of the reducing gas; and/or - wherein the reactor C) for the reduction of an alkaline earth metal sulfate is a rotary kiln and is suitable for continuous operation; and/or - wherein the reactor C) for the reduction of an alkaline earth metal sulfate is a shaft furnace and is suitable for quasi-continuous operation; and/or - wherein the reactor C) for the reduction of an alkaline earth metal sulfate is suitable for operation, preferably continuous operation, at operating temperatures in the range of 400 °C to 1200 °C, preferably in the range of 500 °C to 1100 °C.
13. Production plant according to one of the preceding Claims 10 until 12 , wherein reactor C) for the reduction of an alkaline earth metal sulfate is equipped with: - an inlet opening for bulk solids, - wherein the inlet opening for bulk solids is preferably equipped with a device for measuring the temperature of the bulk solids entering the inlet opening; and/or - wherein the production plant has a device upstream of the inlet opening for bulk solids for measuring the mass and/or volume of the bulk solids entering the inlet opening; and/or - an outlet opening for bulk solids - wherein the outlet opening for bulk solids is preferably equipped with a device for measuring the temperature of the bulk solids exiting the outlet opening; and/or - an inlet opening for reducing gas - wherein the inlet opening for reducing gas is preferably equipped with a device for measuring the temperature of the reducing gas entering the inlet opening; and/or - wherein the production plant is equipped with a device for measuring the mass and/or volume of the reducing gas entering the reactor; and/or - an outlet opening for gaseous reaction byproducts - wherein the outlet opening for gaseous reaction byproducts is preferably equipped with a device for measuring the temperature of the gaseous reaction byproducts exiting the outlet opening; and/or - wherein the production plant is equipped with a device for measuring the mass and/or volume of the gaseous reaction byproducts exiting the outlet opening; and/or - wherein the production plant is equipped with a device for measuring the concentration of substances in the gaseous reaction byproducts exiting the outlet opening.
14. Production plant according to one of the preceding Claims 10 until 13 , wherein reactor C) for the reduction of an alkaline earth metal sulfate is a shaft furnace and - wherein the shaft furnace is suitable for operating temperatures in the range of 400 °C to 1400 °C, preferably in the range of 500 °C to 1200 °C, particularly preferably in the range of 600 °C to 1000 °C, and most preferably in the range of 700 °C to 950 °C; and/or - wherein the shaft furnace is not equipped with devices for the active mechanical transport of solids; and/or - wherein the shaft furnace is designed such that the transport of bulk solids from an inlet opening for bulk solids to an outlet opening for bulk solids occurs by gravity; and/or - wherein the shaft furnace - is equipped with an inlet opening for bulk solids is equipped and - is equipped with an inlet opening for reducing gas, wherein these inlet openings are arranged in such a way that a countercurrent of bulk solids and reducing gases can be generated in the shaft furnace; and/or - wherein the shaft furnace is designed such that the inlet opening for bulk solids is designed as a lock system with movable flaps; and/or - wherein the shaft furnace is equipped with an outlet opening for bulk solids, which is designed as a lock system with movable flaps; and/or - wherein the shaft furnace is equipped with a device for temperature monitoring with which the temperature of the bulk solids exiting through the outlet opening for bulk solids can be determined; and/or - wherein the shaft furnace is equipped with a device for electrically heating the shaft furnace and the solids contained therein.
15. Production plant according to one of the preceding Claims 10 until 14 , wherein reactor C) for the reduction of an alkaline earth metal sulfate is a rotary kiln and - wherein the rotary kiln is suitable for operating temperatures in the range of 500 °C to 1200 °C, preferably in the range of 600 °C to 1100 °C, particularly preferably in the range of 700 °C to 950 °C; and/or - wherein the rotary kiln is equipped with devices for the active mixing of solids and gas phase; and/or - wherein the rotary kiln - is equipped with an inlet opening for bulk solids and - is equipped with an inlet opening for reducing gas, these inlet openings being arranged such that a countercurrent of bulk solids and reducing gases can be generated in the rotary kiln; and/or - wherein the production plant is designed such that a lock system, preferably a lock system with movable flaps, is located upstream of the inlet opening for solids of the rotary kiln; and/or - wherein the production plant is equipped with an outlet opening for bulk solids, designed as a lock system; and/or - wherein the rotary kiln is equipped with a device for temperature monitoring with which the temperature of the bulk solids exiting through the outlet opening for bulk solids can be determined; and/or - wherein the rotary kiln is equipped with a device for electrically heating the rotary kiln and the solids contained therein.
16. Use of hydrogen and/or methane, preferably use of hydrogen, in a process for the production of an alkaline earth metal compound other than an alkaline earth metal sulfate, preferably an alkaline earth metal carbonate, preferably an alkaline earth metal carbonate selected from the group consisting of barium carbonate and strontium carbonate, wherein the process is preferably a process according to one of the preceding Claims 1 until 9 is.
17. Kit for the production of an alkaline earth metal compound other than an alkaline earth metal sulfate, preferably for the production of an alkaline earth metal carbonate, particularly preferably for the production of an alkaline earth metal carbonate selected from the group consisting of: barium carbonate and strontium carbonate, comprising at least: - a sulfate compound, preferably barium sulfate and/or strontium sulfate; and - a reducing gas, preferably methane and/or hydrogen, particularly preferably hydrogen.
18. Use of a kit in accordance with the above Claim 17 for the production of an alkaline earth metal compound other than an alkaline earth metal sulfate, preferably for the production of an alkaline earth metal carbonate, particularly preferably for the production of an alkaline earth metal carbonate selected from the group consisting of: barium carbonate and strontium carbonate, wherein the process is preferably a process according to one of the preceding Claims 1 until 9 is.

Description

The present invention relates to a process for the industrial production of an alkaline earth metal compound other than an alkaline earth metal sulfate. The present invention also relates to a production plant for the production of an alkaline earth metal compound other than an alkaline earth metal sulfate. The present invention further relates to the use of hydrogen and/or methane in a process for the production of an alkaline earth metal compound other than an alkaline earth metal sulfate. The present invention further relates to a kit for the production of an alkaline earth metal compound other than an alkaline earth metal sulfate. The present invention also relates to the use of such a kit. The present invention lies in the field of the industrial production of alkaline earth metal compounds that are not alkaline earth metal sulfates. Such alkaline earth metal compounds differ fundamentally in their properties and industrial production from metals such as iron, aluminum, copper, gold, and others. It is known to those skilled in the art that the knowledge gained from the industrial production processes of these metals, in particular the knowledge gained from the industrial production processes of iron from iron ore, cannot be transferred to the industrial production of alkaline earth metal compounds that are not alkaline earth metal sulfates without an unreasonable effort. The industrial production (i.e., production of more than 100 kg per hour) of alkaline earth metal compounds other than alkaline earth metal sulfates differs fundamentally in its requirements from the production of corresponding compounds on a laboratory scale (i.e., production from a few mg per hour to 1000 g per hour). It is known to those skilled in the art that scaling up a production process from laboratory scale to an industrial production process is regularly associated with complex development steps; for example, it is known that the material distribution in the reaction chamber, the transport of reactants and products in the reaction chamber, the spatial distribution of heat generation in the reaction chamber, the implementation of possible cooling and/or heating steps in the reaction chamber, the distribution of additionally supplied reactants in the reaction chamber, the control of reaction kinetics, and other factors differ fundamentally in industrial production processes compared to those on a laboratory scale. The industrial production of alkaline earth metal compounds that are not alkaline earth metal sulfates is carried out according to the prior art starting from the respective alkaline earth metal sulfates by reducing the alkaline earth metal sulfates with solid coke (carbon / petroleum coke) to the corresponding alkaline earth metal sulfides and subsequently processing the alkaline earth metal sulfides into the desired alkaline earth metal compounds. The industrial production of alkaline earth metal compounds other than alkaline earth metal sulfates is currently associated with CO₂ production, which is increasingly considered problematic in the field of the present invention due to the climate-damaging effects of CO₂ . Therefore, there is a need for processes for the industrial production of alkaline earth metal compounds other than alkaline earth metal sulfates that release as little CO₂ as possible during production. In particular, there is also a need for processes for the industrial production of alkaline earth metal compounds other than alkaline earth metal sulfates that release no CO₂ at all during production. There is also a need for processes for the industrial production of alkaline earth metal compounds that are not alkaline earth metal sulfates, which can be carried out using readily available starting materials in sufficient quantities. There is also a need for processes for the industrial production of alkaline earth metal compounds that are not alkaline earth metal sulfates, whereby no additional process steps involving disproportionately high costs are required compared to the processes known from the prior art. Capturing and subsequently storing the resulting CO2 is often associated with an undesirably high level of effort and is therefore undesirable in many cases in the field of the present invention. There is also a need for processes for the industrial production of alkaline earth metal compounds that are not alkaline earth metal sulfates, in which a reducing agent is used, the transport of which to the place of process execution is carried out with the lowest possible CO2 emissions. There is also a need for processes for the industrial production of alkaline earth metal compounds other than alkaline earth metal sulfates, in which the resulting intermediate products can be purified with minimal equipment and/or time expenditure. In particular, there is a need for processes for the industrial production of these compounds. of alkaline earth metal compounds that are not alkaline earth metal sulfates,