EP2482971A1

EP2482971A1 - Mineral, granulated desulfurizing agent on the basis of calcium hydroxide, method for the production thereof and use thereof

Info

Publication number: EP2482971A1
Application number: EP10770738A
Authority: EP
Inventors: Torsten Schlicht; Dirk Dombrowski
Original assignee: Individual
Current assignee: Individual
Priority date: 2009-10-02
Filing date: 2010-09-08
Publication date: 2012-08-08
Also published as: DE102009045278A1; DE102009045278B4; WO2011039034A1; CA2774942A1; US20120235086A1

Abstract

The invention relates to a mineral desulfurizing agent (10), comprising calcium-based porous granules (12) which comprise a core (14) containing at least 80% by weight of calcium carbonate (CaCO₃) and at least one agglomeration layer (16) enveloping the core (14) and containing calcium hydroxide (Ca(OH)₂), wherein the granules (12) have a proportion of calcium hydroxide (Ca(OH)₂) of at least 60% by weight relative to the total dry weight of the granules (12), an essentially spherical shape and a BET surface area of at least 8 m²/g. The invention further relates to a method for the production and use of a mineral desulfurizing agent.

Description

Mineral granular desulphurising agent based on calcium hydroxide, process for its preparation and its use

The invention relates to a mineral porous desulphurising agent produced by granulation, which can be used in particular for separating the oxides of sulfur from combustion exhaust gases. The invention further relates to a process for the preparation of the desulphurising agent and to the use of the desulphurising agent.

Fossil fuels, such as lignite, peat, hard coal, petroleum, but also in marine engines usable fuels containing sulfur compounds in varying amounts, which are oxidized in the combustion of fuels predominantly to sulfur dioxide and in small quantities to sulfur trioxide. The resulting in the combustion of fossil fuels exhaust gases therefore contain up to 10,000 mg S0 ₂ per standard cubic meter (Nm ³ ) exhaust gas, the exhaust gases of a powered with residual oils marine engine can contain up to 5000 mg S0 ₂ / Nm ³ . Sulfur oxide-containing exhaust gases, however, also occur in other thermal processes, such as in waste incineration plants, hazardous waste incineration plants and biomass incineration plants. Since the oxides of sulfur act as environmental toxins and can react in the atmosphere to "acid rain", it is necessary to remove the sulfur oxides from the exhaust gases of combustion processes.

In the field of exhaust gas purification, numerous processes are used, including wet and dry processes. In dry exhaust gas purification processes it is known to contact combustion exhaust gases with solid desulphurisation agents, the oxides of sulfur reacting with the desulphurising agent to form solid sulphates and sulphites and being retained in this form. Calcium oxide, calcium hydroxide, and calcium carbonate are used in particular as solid desulfurizing agents which essentially react with S0 ₂ and S0 ₃ at elevated temperature and at different temperature ranges in the presence of oxygen to form calcium sulfate. This can be in suitable filtering separators, such as electrostatic precipitators or bag filters are deposited with textile filter materials. The reactivity of the desulfurizing agents is defined in particular by their particle size, their porosity and their mechanical strength. Some desulphurising agents are blown directly into the combustion chamber (eg limestone). On the other hand, other desulfurization agents are reacted with the sulfur oxides of the combustion gas in a post combustion solid-gas reaction. The disadvantage of this so-called flight flow method lies in the temperature limitation of the filtering separator, in particular the bag filter, which can not be operated at temperatures above 240 ° C.

Desulphurization processes of combustion exhaust gases, which usually have temperatures between 240 and 450 ° C, can only be operated with packed bed filters, which in turn can not be operated with powdered desulfurization, since they can only be used with technically unacceptable pressure losses.

In the dry exhaust gas purification, basic additives, e.g. Calcium hydroxide and limestone, blown in powder form in the furnace or exhaust gas stream and then deposited on filtering separators. Often, a conditioning of the exhaust gases by Quentschung or by feeding water vapor takes place. In WO 92/06772 A1, such a dry process is described in which improvements in the degree of separation are possible by setting high relative humidity due to a reduction in the temperature of the exhaust gas stream. Nevertheless, with such a process at a temperature of 70 ° C. and a stoichiometric ratio of basic additive to noxious gas of 2: 1, only degrees of precipitation of 60% are achieved.

DE 37 16 566 A1 proposes, in order to improve the separation efficiency, to modify the calcium hydroxide by adding substances to the extinguishing water during the deletion process of the quicklime, which should increase the reactivity of the calcium hydroxide formed during the extinguishing process. As additives to be considered, calcium chloride and magnesium chloride are mentioned. In this connection, it is believed that because of the calcium chloride's tendency to absorb water, water does not enter the granular interior of the calcium hydroxide, ultimately leading to an increase in its reactivity. However, attempts by the present inventors could not confirm the theory set forth in this document. It has rather, it has been found that the very presence of water on the solid surfaces, such as in the form of water vapor sorption layers, results in increased conversion of the calcium hydroxide with sulfur dioxide. A disadvantage of the described in DE 37 16 566 A1, modified particles of calcium hydroxide is also associated with the production of high costs, which is why a process performed therewith for exhaust gas purification leads to high operating costs and has low flexibility in terms of fluctuations in the exhaust gas composition. Another disadvantage is that the proposed particles can not be used in a fixed bed absorber.

In DE 39 15 934 A1 a method for exhaust gas purification is described in which the reactive calcium hydroxide surfactants are added. These substances are characterized by a particularly large in terms of their weight surface. As an example activated carbon with 700 m ² / g active surface is called. The addition of surfactants may be before, during, or after the quenching of the calcium hydroxide. The aim of this modification is to improve the separation of heavy metals and dioxins / furans from flue gas. Surface-active substances, as proposed in DE 39 15 934 A1, however, only partly participate in the deposition of sulfur oxides and can not be used at temperatures above 300 ° C., since the ignition temperature of activated carbon is exceeded.

A similar process, in which also a modification of the calcium hydroxide is carried out, is known from DE 40 33 417 A1. In this case, aggregates with a highly porous structure and a correspondingly increased reactive surface area are used. As in the method according to DE 39 15 934 A1, the aim is to deposit in particular heavy metals and organic pollutants by the addition of substances having a large specific surface area. However, for a sulfur oxide deposition process, the use of these highly reactive substances is not economical.

EP 0 387 928 A2 proposes a desulphurising agent consisting of calcium hydroxide with 3 to 10% by weight lignite ash and used in pelleted form, the pellets having a diameter of 0.2 to 3 mm, preferably 0.5 to 1 mm, and at about 750 to 950 ° C in the firing space, such as a circulating fluidized bed, are introduced. Pellets or granules of this diameter can not be used in a fixed-bed absorber because the air permeability of such a bed is too low and the pressure drop over the fixed bed absorber reaches a technically not permissible level.

Also known are porous mineral granules for adsorption and absorption of liquids and gases. DE 195 09 747 A1 proposes a granulate whose grain size is between 0.5 and 4 mm, preferably between 0.5 and 2 mm, and is to be used as hygiene animal litter. EP 0 716 806 A1 likewise discloses granules for use as animal litter which have particle sizes of <0.5 mm. Furthermore, DE 198 43 887 B4 discloses a hygiene granulate based on calcium silicate and bentonite, according to which the granules have pelletized granules with a two-layer structure with a core and a shell or a shell, the core predominantly calcium silicate hydrate and the shell has a mixture of finely divided, swellable clay mineral and finely divided calcium silicate hydrate. Such granules are unsuitable for the desulphurisation of exhaust gases.

The dosage of the solid desulfurizing agents which bind the oxides of sulfur in a gas-solid reaction is problematic because the desulfurizing agents often have to be used in finely divided form because of the required reactivity, but this is associated with disadvantageous flow and agglomeration behavior , There has therefore been no lack of attempts to use the desulfurization in particulate or pelletized form, which in many cases a reduction in reactivity is connected, because not infrequently, the effective agent of the desulfurization must in three- to six-fold stoichiometric excess, based on the sulfur content of Exhaust gases, are used.

Another disadvantage is that powdered desulfurizing agents can not be used in fixed bed or moving bed absorbers because the pressure losses in a fixed bed absorber would rise to an uneconomic level and the advantage of the higher operating temperature of> 300 ° C and the associated higher reactivity of the desulfurizing agent, especially the calcium hydroxide, would consume again.

The object of the invention is to provide a desulfurizing agent which is suitable for dry exhaust gas purification and which can be used in particulate, pelletized or granulated form in packed bed filters, fixed bed absorbers and moving bed absorbers has high absorbency and high reactivity with respect to the conversion of sulfur oxides SO _x . The desulfurizing agent should further have high mechanical strength, good abrasion resistance and large reactive surface area and high temperature resistance of at least up to 500 ° C. Likewise, the agent should be dimensionally stable and mechanically strong even after the chemical reaction. Furthermore, the granules should not be toxic, environmentally friendly and easily conveyed by eg pneumatic conveyors or chain conveyors. Furthermore, a process for the preparation of the desulfurizing agent is to be made available. These objects are achieved by a mineral desulfurizing agent, a process for its preparation and its use with the features of the independent claims. Preferred embodiments of the invention are the subject of the independent claims. Have the inventive mineral desulfurizing agent comprising calcium-based porous granules, the core has an at least 80 wt .-% of calcium carbonate (CaC0 _3), containing and at least one, surrounding the core, and calcium hydroxide (Ca (OH) ₂₎ containing agglomerate layer. The granules have a proportion of at least 60% by weight of calcium hydroxide (Ca (OH) ₂ ) based on the total dry mass of the granules. In addition, the granules have a substantially spherical shape and a BET surface area of at least 8 m ² / g, in particular from 8 to 60 m ² / g, preferably from 15 to 45 m ² / g.

It has surprisingly been found that such granules, which essentially consists of calcium hydroxide-based granules, have very good absorption properties with regard to sulfur oxides and, after the chemical reaction with calcium sulfate, retain their mechanical properties with regard to strength and abrasion resistance. The granules of the granules have a very high stability for use as bulk material and a good flowability and allow the use as a filler in a packed bed filter, fixed bed reactor or moving bed reactor.

Granules which form the granulate (desulfurizing agent) according to the invention are in the context of the invention intrinsically solid granular products which are produced by a material-applying, agglomerating granulation process and not by a material-removing process, such as breaking or grinding. By the agglomerating granulation process grains are obtained, one for the intended use have good to very good, abrasion resistant mechanical strength. Thus, the granules are well funded. Due to the production of the granules results in a relatively narrow particle size range, typically with Gaussian grain distribution, wherein the granules have approximately a uniform geometric shape, which corresponds to a spherical shape and / or approximate spherical shape. In this context, a particle size distribution with diameters in the range of 1 to 20 mm, in particular in the range of 2 to 8 mm, preferably from 3 to 6 mm, has proven particularly useful. Due to the spherical shape, the granules have no abradable edges, resulting in little abrasion during conveyance or use.

The mineral desulphurising agent according to the invention can be prepared by a process in which a mixture comprising at least calcium hydroxide (Ca (OH) ₂ ) in the form of powder and grains containing at least 80 wt .-% calcium carbonate (CaC0 ₃ ) (the so-called "Ergot"), and water is added in a granulation or Pelltiermischer, granules are produced by granulation and the granules thus produced are dried.

Thus, the granules can be wholly made of powder containing at least calcium hydroxide and granular CaCO ₃ material and water, as granules having rounded surface contours. The equivalent terms "powdery" or "dusty" in the context of the present invention mean very finely divided particle sizes in normal, production-related particle size distribution. On the other hand, "granular" tends to mean larger particle sizes. "Finely divided fractions" are understood to mean primarily the term "powder" or "pulverulent." Furthermore, the term "mixed material" is understood here to mean the total of the dry constituents, comprising the calcium hydroxide powder and the calcium carbonate ergot and optionally other components listed below, ie all components except the liquid phase, which preferably consists exclusively of water. According to a first embodiment of the invention, the powder of at least one calcum umstämmigen material and the mother grain in a so-called pelletizer or granulation (both terms are equivalent) and mixed in the mixer during mixing with water, for example sprayed or sprayed with this , In an alternative embodiment, the dry mix or part of it is mixed before the task in the mixer with a part or with the total amount of water. In the pelleting mixer or granulation mixer, granulation or pelletization is then carried out. dung. The terms "granulation", "built-up granulation", "agglomeration" or "pelleting" are treated equivalently in the context of the present invention and designate the material-applying layer structure of the granules. After reaching a granulate with a defined granule size and / or granule size distribution of the granules, the granules are removed from the pelleting mixer and dried.

The Granuliermischer can be configured in particular in the form of a rolling drum whose axis of rotation is inclined only slightly against the horizontal, or a likewise inclined granulating.

The agglomeration principle of the build-up granulation will now be explained using the example of a granulating mixer comprising an inclined granulating plate. However, the principle does not differ in the case of using a roller drum as Granuliermischer. The dosed granulated material is captured by the rotating disc surface and moved upwards, from where it rolls alone or by means of a scraper from the plate surface down to the plate edge. In the process, the calcium carbonate grains (ergot) acting as the primary particles first attract particles of the powder fraction over which they roll by means of adhesion forces, resulting in the formation of primary agglomerates. The downwardly moving and growing primary agglomerates run transversely to the circular paths which describe the points of the disc surface. The rotational movement of the plate thus forces the aggregates which are being rolled by gravity to produce an additional rotational movement. The granule grows in the form that the diameter increases in layers. Once at the bottom, the now somewhat grown agglomerate is picked up from the edge of the plate and conveyed back up again to immediately roll down again, with another layer of the powder fraction "growing up" on the surface of the agglomerate Duration of granulation, during which almost all the primary particles are taken up by agglomerates, which agglomerate into a spherical shape by continuous rolling, whereby the structure of the spherical granules becomes dense, and this compaction turns some of the granulating liquid (water) out of the granules This phenomenon is called by the practitioner the "sweating" of the so-called green granules and is preferred in the context of the invention as a sign of the end of the granulation process. Well compacted granules are held together so strongly by adhesion and cohesion forces that the so-called "green fines" are sufficient for undamaged transport to the next process step, the drying process. According to a preferred embodiment of the method, a calcium hydroxide powder is used, which has a particle size distribution in the range of 1 to 200 μηη. A particularly suitable calcium hydroxide powder has the following particle size distribution:

> 50 to <125 μηι 3 to 8 wt .-%

> 15 to <50 μηι 20 to 33 wt .-%

> 5 to <15 μηη 40 to 57 wt .-%

<5 μηη 20 to 35 wt .-%

The calcium hydroxide powder preferably has the following particle size distribution:

> 50 to <125 μηι 4 to 7 wt .-%

> 15 to <50 μηι 23 to 27 wt .-%

> 5 to <15 μηι 42 to 48 wt .-%

<5 μηη 23 to 27% by weight

It has been found that calcium hydroxide powder can be granulated particularly well, which is used promptly after its deletion.

The granulation process is particularly good if the ergot has a mean particle size of 40 to 150 μηη, in particular from 45 to 125 μηη, preferably from 50 to 85 μηη. In other words, the ergot is used with a grain size that tends to be larger than that of the calcium hydroxide, thus acting as a nucleus for the granulation process described above.

In addition, a proportion of the ergot based on the total dry mix (which corresponds to the proportion of ergot in the total dry matter in the product) in the range of 0.05 to 15 wt .-%, in particular in the range of up to 0.1 to 10 wt .-%, preferably in the range of 0.1 to 5 wt .-%, particularly preferably in the range of 0.1 to 3 wt .-%, proven. In particularly advantageous examples, the proportion is about 1 wt .-%. Typically, the ergot has a purity with respect to the calcium carbonate of> 85 wt .-%, in particular> 90 wt .-%, preferably> 95 wt .-% to. As described above, the ergot has mainly the function to initialize the agglomeration process, which works particularly well in the above areas in the sense that virtually all the ergot is absorbed, at the same time Powder material is largely completely consumed and suitable granule diameter can be achieved.

The liquid phase used is preferably exclusively water, which is preferably metered into the mix to be granulated during mixing. The water can be used in amounts of 10 to 50 wt .-% based on the total approach, in particular in the range of 20 to 45 wt .-%. A preferred water content is 30 to 40 wt .-%, in particularly preferred examples 32 to 38 wt .-%, each based on the total granulation. The water can be added, for example, by spraying or injecting into the mixer, with relatively little mixing energy causing granulation in the mixer. In this case, the mixing component parameters, the amount of granulation and in particular the proportion of water are adjusted so that a free-flowing granules is produced with relatively good green strength, whose spatial form is substantially rounded, i. is substantially spherical and has water contents in the amounts indicated above.

The drying process can take place, for example, in the fluidized-bed dryer or belt dryer. The drying conditions (especially temperature and duration) are chosen so that a water content after drying in the range of 2 to 20 wt .-%, in particular from 3 to 15 wt .-%, preferably from 4 to 10 wt .-% and in particularly advantageous examples 3 to 8 wt .-%, is, in each case based on the total mass of the granules (including the water content). The bulk density of the granules after drying is in particular in the range from 600 to 900 g / l, preferably in the range from 750 to 850 g / l.

The product of drying, i. the granules according to the invention may be microporous with pore diameters smaller than 100 μm or mesoporous with pore diameters in the range of 100 and 500 μm or macroporous with pore diameters above 500 μm. Typically, pore diameters are present in several of the aforementioned categories.

After the drying process, the granule diameters are typically in the range of about 0.5 to 30 mm, from which the desired particle size range can be separated in a screening process following the drying step. Granules having a particle size distribution with diameters in the range of 1 to 20 mm, in particular in the range of 2 to 8 mm, are preferably used from 3 to 6 mm, isolated and used for the particular application, for example as a bed.

In order to obtain an even firmer composite of the granules, one or more binders can also be added to the mix, so that the binder is contained in the finished granules in the at least one agglomeration layer grown on the core (ergot). The at least one binder is in particular selected from the group of the cellulose ethers, in particular the carboxylmethylcelluloses, especially the alkali metal or alkaline earth metal carboxylmethylcelluloses, for example sodium, potassium and calcium carboxymethylcellulose. Likewise, molasses can be used as a binder alone or in combination with other binders. Suitable proportions of the binder are in the range of 0.05 to 2 wt .-%, in particular from 0.1 to 1 wt .-%, preferably in the range of 0.2 to 0.5 wt .-%, based on the total Dry mix, so that in the finished product, this proportion based on the total dry mass of the granules is present.

The binder (s) can already be mixed in initially with the mixture so that in the finished granule the at least one agglomeration layer contains the binder in a substantially homogeneous distribution. In a preferred embodiment, however, the binder is not added to the mixer until later in the course of granulation, when the bulk of the powder has already been taken up by the granules. This Nachgranulierprozess may be useful for binding of sometimes existing residual powder on the granules. In this variant, granules are formed in which the inner Agglomensationsschichten are virtually free of binder and contain only the outer Agglomensationsschichten binder.

It is within the scope of the invention, in addition to the calcium hydroxide (Ca (OH) ₂ ) further desulfurizing agent, for example magnesium hydroxide (Mg (OH) ₂ ), calcium oxide (CaO), calcium carbonate (CaC0 ₃ ) and / or sodium bicarbonate (NaHC0 ₃ , also Natriumbi - called carbonate), which can be added in powder form to the mix before and / or during granulation. In this case, advantageous proportions of the further desulfurizing agent or in the range of up to 30 wt .-%, in particular from 1 to 15%, preferably from 5 to 10 wt .-%, each based on the total dry matter of the granules. Preferably, the sum of all further used desulfurizing agent used does not exceed said limits. Furthermore, alternatively or additionally, surface-active substances which absorptively bind sulfur oxides, as Herdofenkoks and / or activated carbon, preferably in amounts of up to 35 wt .-%, in particular 1 to 15 wt .-%, preferably from 5 to 10 wt .-%, in turn, based on the dry total mass of the granules are added. The additional desulfurizing agents and / or surface-active substances are present in the finished granule as part of the agglomeration layer / s in the specified concentration ranges.

Although the abovementioned additional desulfurizing agents and / or surface-active substances are encompassed by the present invention, the highest possible proportion of calcium hydroxide in the powder fraction (or in the at least one agglomeration layer in the finished granulate) is preferred. In this case, a calcium hydroxide content in the total dry mass of the granules of 60 to 99.95 wt .-%, in particular from 70 to 99.90 wt .-%, preferably from 80 to 99.90 wt .-% is preferred. In particularly preferred examples, the proportion is 90 to 99.5 wt .-%, in particular 97 to 99 wt .-%. In this case, a calcium hydroxide powder having a purity of at least 85 wt .-%, in particular of at least 90 wt .-%, preferably at least 94 wt .-% find use.

A granulate produced according to a preferred embodiment of the invention has granules consisting of:

82 to 97 wt .-% calcium hydroxide

3 to 14 wt .-% adsorptively bound water, after drying

0.1 to 3 wt .-% calcium carbonate

0 to 1% by weight of carboxymethylcellulose,

An even more preferred granules according to the invention has the composition

90 to 96 wt .-% calcium hydroxide

3 to 8 wt .-% adsorptively bound water, after drying

0.5 to 1 wt .-% calcium carbonate

0 to 0.5% by weight of carboxymethylcellulose, with traces of impurities typically contained in these ingredients. The mineral desulfurizing agent according to the invention as described above can be used with particular advantage for the desulphurisation of exhaust gases from combustion processes, in particular combustion engine exhaust gases. Since the desulfurization agent according to the invention is characterized by a high absorption of sulfur oxides even at relatively low temperatures, the exhaust gas desulfurization can be carried out with particular preference in a wide temperature range of 100 to 900 ° C, preferably from 130 to 450 ° C. This corresponds to typical exhaust gas temperatures in a whole operating range of internal combustion engines, especially large marine diesel engines.

Advantageously, the mineral desulfurizing agent may also be used to remove hydrogen chloride HCl and / or hydrogen fluoride HF from exhaust gases from combustion processes, with neutralization of these exhaust gas constituents taking place. Hydrogen chloride and hydrogen fluoride are produced, for example, in coal-fired kettles or waste incineration plants.

Due to its very good mechanical stability, its high compressive strength and its low abrasion, the desulfurization agent according to the invention can be used as a charge in packed bed filters, fixed bed absorbers or moving bed absorbers through which the combustion exhaust gas flows.

The invention will be explained in more detail in an embodiment. (1) Preparation of granules

There were 800 g of calcium hydroxide powder (Ca (OH) ₂ content> 94 wt .-%), of which 20 to 35 wt .-%, a particle size of <5 μηη, 40 to 57 wt .-%, a particle size of> 5 to <15 μηι, 20 to 33 wt .-% of a particle size of> 15 to <50 μηη and 3 to 8 wt .-% had a particle size of> 50 to <125 μηη, a Granuliermischer with a turntable abandoned. This powder fraction was first premixed by continuous sprinkling of the mix with water to a slurry, with a total of 500 g of water were added. Only then 10 g of ergot, the CaC0 ₃ grains having a CaC0 ₃ content of> 95 wt .-% and a particle size distribution in the range of 60 to 125 μηη had added to the slurry. After most of the material had been taken up by the resulting agglomerates, 2 g of sodium carbohydrate were added. xylmethylcellulose was added to the mixer and the batch continued until all of the material was taken up by the granules and the so-called "sweating" of the granules, ie incipient shining, indicated the displacement of the water from within the agglomerates The granules thus obtained had a particle size distribution in the range from 0.5 to 25 mm, and in a subsequent sieving process, the particle size range from 3 to 6 mm was isolated and analyzed for The single figure shows in a schematic and not true to scale representation the structure of a typical desulfurizing agent thus obtained and designated overall by the reference numeral 10. Three granules 12 are shown in a sectional view by way of example Pictured llten core 14, which corresponds to the ergot used and thus essentially consists of CaC0. ₃ Thus, the diameter d _{K of} the core 14 corresponds to the mean grain size of the ergot used. Arranged around the core 14 in a substantially concentric arrangement is a plurality of agglomeration layers 16, which consist essentially of Ca (OH) ₃ and may optionally contain further constituents, in particular binders, such as carboxylmethylcellulose. According to the above embodiment, the carboxylmethyl cellulose is present exclusively in the outer agglomeration layer (s) 16 and results in an increase in the cohesion and abrasion resistance of the granules 12.

(2) Material properties of the granules

The spatial form of this granules 12 produced according to the embodiment (1) was well rounded and independent of the typical particle size distribution of the calcium hydroxide powder used. The mean grain size d _{G of} the granules was about 5 mm. Particularly advantageous in this embodiment was the surface structure of the granules, which consisted of a system of micro-, meso-, and macropores and had a mean pore size of about 0.03 μηη with a BET surface area of about 42 m ² / G. In Table 1, some material sizes of the inventive granules prepared according to Example (1) are compiled in comparison to commercially available desulfurizing agents.

Table 1: Properties of granulated desulphurising agent Desulphurisation Composition Porosity Specific median mean (%) Surface pore size

(Dry matter)

(m ² / g) (mm)

Limestone> 95% CaC0 ₃ 19.3 2.9 0.54

Comparative A A 10-20% Ca (OH) ₂ 27.0 7.3 0.06

80-90% CaC0 ₃

5% others

Comparative Agent B 40-45% Ca (OH) ₂ 32.1 24.5 0.04

40-45% CaC0 ₃

10% others

Example (1)> 93% Ca (OH) ₂ 39.9 42.2 0.03

> 1, 2 CaC0 ₃

<5.8% others

(3) Investigation of the absorption behavior of the granules with respect to S0 ₂

The granules according to the invention produced according to Example 1 were examined with respect to its absorption properties in comparison to the prior art materials from Example 2 at 100, 200 and 300 ° C respectively. For this purpose, a method was developed with which the relative absorption rates of natural and synthetic materials can be compared. In this process, absorbent granules are exposed to a synthetic S0 ₂ containing flue gas at selected temperatures. The amount of acid gas absorbed is determined by a combination of simultaneous thermal analysis and analysis of the released gas. The materials to be examined were dried and classified. The surface area, density and porosity of each sample were determined and the chemical composition of each absorbent was calculated by thermal analysis. A Netzsch STA 449C Simultaneous Thermal Analyzer (TG / DSC) coupled to a Bruker Vector 22 FTIOR (Fourier Transform Infrared Spectrometer) for the released gas analysis was used to measure the characteristic weight losses for both CaC0 ₃ and Ca (OH) ₂ is used. The CaCO ₃ and Ca (OH) ₂ levels were calculated by comparing the weight loss after heating of each absorbent with the theoretical weight loss for each material. The relative absorption efficiencies Tenets for each material were measured using the coupled thermal analysis system. For these measurements, the simultaneous thermal analyzer was operated with a large sample platform that allows only thermogravimetric measurements. The S0 ₂ had a concentration of 1800 ppm in dry nitrogen. For the absorption studies, baselines were first formed for the three temperature ranges. The primary infrared absorption band of S0 ₂ was measured several times per minute. In order to minimize the overlap between the absorption bands of water vapor and SO ₂ , drying gases were used. After development of the baseline, each sorbent was exposed to S0 ₂ under conditions identical to those for the baseline. The difference between the baseline recording and the absorbance recording by the sample was used to calculate the absorption rate of SO ₂ by the absorbent. For the tabulated absorbance values, a linear approximation (average) was used to determine a single absorption rate for the material. The results are shown in Table 2. It has surprisingly been found that the granulated desulfurizing agent according to the invention by far the highest deposition rates based on S0 ₂ .

Table 2: S0 ₂ absorption data for granulated desulphurising agents

# Absorbed amount S0 ₂ per g of absorbent

§ Absorbed amount S0 ₂ per ml of absorbent The results not only show that the mineral desulfurizing agent according to the invention has significantly higher absorption values at all the temperatures tested, but that the absorption, in contrast to the comparison materials, is characterized by a very high absorption rate even at the relatively low temperature of 100 ° C.

It was also surprisingly observed that during the absorption of S0 ₂ an initial peak occurs which was followed by a decreasing rate of absorption. This suggests that, after the surface of the granule is saturated with SO ₂ , the reaction rate is controlled by the diffusion of SO ₂ through the reaction layer. Therefore, it is advantageous according to the invention to produce a granulate which is characterized by a large porosity and capillarity.

LIST OF REFERENCE NUMBERS

desulfurization

granule

core

agglomeration layer

Diameter of core / ergot size Granule grain size

Claims

A mineral desulfurizing agent (10) comprising calcium-based porous granules (12) containing a core (14) containing at least 80% by weight of calcium carbonate (CaCO ₃ ) and at least one core (14) enveloping and calcium hydroxide-containing ( Ca (OH) ₂ ) Agglomerationsschicht (16), wherein the granules (12) has a proportion of calcium hydroxide (Ca (OH) ₂ ) of at least 60 wt .-% based on the total dry mass of the granules (12), a substantially spherical shape and a BET surface area of at least 8 m ² / g.

Desulfurizing agent (10) according to claim 1, wherein the granules (12) has a water content of 2 to 20 wt .-%, in particular from 3 to 15 wt .-%, preferably from 4 to 10 wt .-%, each based on the total mass of the granules (12).

Desulphurising agent (10) according to one of the preceding claims, wherein the at least one agglomeration layer (16) in addition to calcium hydroxide further at most 30 wt .-%, in particular 1 to 15 wt .-%, preferably 5 to 10 wt .-%, of at least one further desulfurizing agent contains in each case based on the total solids of the granules (12), selected from magnesium hydroxide (Mg (OH) ₂ ), calcium oxide (CaO), calcium carbonate (CaC0 ₃ ) and sodium bicarbonate (NaHC0 ₃ ).

Desulfurizing agent (10) according to any one of the preceding claims, wherein the at least one agglomeration layer (16) further contains at most 35 wt .-%, in particular 1 to 15 wt .-%, preferably 5 to 10 wt .-%, of at least one surface-active substance respectively based on the total dry mass of the granules (12) selected from hearth furnace cokes and / or activated carbon.

Desulfurizing agent (10) according to any one of the preceding claims, wherein the granules (12) has a calcium hydroxide content of 60 to 99.95 wt .-%, in particular from 70 to 99.9 wt .-%, preferably from 80 to 99.5 Wt .-%, particularly preferably 90 to 99 wt .-%, based on the total dry weight of the granules (12).

6. desulfurizing agent (10) according to any one of the preceding claims, wherein at least one outer agglomeration layer (16) further contains at least one binder which is selected from the group of cellulose ethers, in particular the Carboxylmethylcellulosen, and / or molasses.

7. desulfurizing agent (10) according to any one of the preceding claims, wherein the granules (12) have micropores with pore diameters of less than 100 μηη, mesopores with pore diameters of 100 to 500 μηη and / or macropores having pore diameters above 500 μηη ,

8. desulfurizing agent (10) according to any one of the preceding claims, wherein the granules (12) has a particle size distribution with diameters (d _G ) in the range of 1 to 20 mm, in particular in the range of 2 to 8 mm, preferably from 3 to 6 mm, exhibit.

9. desulfurizing agent (10) according to any one of the preceding claims, wherein the granules (12) have a BET surface area in the range of 8 to 60 m ² / g, in particular in the range of 15 to 45 m ² / g.

10. desulfurizing agent (10) according to any one of the preceding claims, wherein desulfurizing agent (10) has a bulk density in the range of 600 to 900 g / l, in particular in the range of 750 to 850 g / l. 1 1. A process for producing a mineral desulfurizing agent (10) according to any one of claims 1 to 10, wherein a mixed material, the oxide of at least Calciumhydro- (Ca (OH) ₂₎ in the form of powder as well as a, at least 80 wt .-% of calcium carbonate (CaC0 ₃ ) and adding water in a granulation or Peller mixer, granules (12) are produced by granulation and the granules (12) thus produced are dried.

12. The method of claim 1 1, wherein the calcium hydroxide powder has a particle size distribution in the range of 1 to 200 μηη, wherein in particular 20 to 35 wt .-%, a particle size of <5 μηη, 40 to 57 wt .-% a particle size of > 5 to <15 μηη, 20 to 33 wt .-% of a particle size of> 15 to <50 μηη and 3 to

8 wt .-% have a particle size of> 50 to <125 μηη.

13. The method according to any one of claims 1 1 or 12, wherein the water in a proportion of 10 to 50 wt .-%, in particular from 20 to 45 wt .-%, preferably from 30 to 40 wt .-%, particularly preferably from From 32 to 38 wt .-%, based on the dry mix is used.

14. The method according to any one of claims 1 1 to 13, wherein the water is added during mixing to the mix in the mixer, in particular sprayed, or is premixed before the task with at least one component of the mix.

15. The method according to any one of claims 1 1 to 14, wherein the drying process is carried out in a fluidized bed dryer or belt dryer.

16. The method according to any one of claims 1 1 to 15, wherein the ergot has a mean grain size (d _K ) in the range of 40 to 150 μηη, in particular from 45 to 125 μηη, preferably from 50 to 85 μηη having.

17. The method according to any one of claims 1 1 to 16, wherein a proportion of the ergot based on the dry mix in the range of 0.05 to 15 wt .-%, in particular in the range of 0.1 to 10 wt .-% , preferably in the range of 0.1 to

5 wt .-%, more preferably in the range of 0.1 to 3 wt .-%, is.

18. Use of a mineral desulfurizing agent (10) according to any one of claims 1 to 10 for the removal of sulfur and / or hydrogen chloride and / or hydrogen fluoride from exhaust gases of combustion processes, in particular at a temperature of 100 to 900 ° C, preferably from 130 to 450 ° C.

19. Use according to claim 18, wherein the desulfurizing agent (10) is used as a bed in bulk-material filters through which the combustion exhaust gas flows, fixed bed absorbers or moving bed absorbers.