DK176546B1 - Dust-free, dispersible compacted or briquetted carbon@ black for colouring building or organic materials - made using processing aid by compacting, pulverising and separating into fractions - Google Patents

Abstract

Production of compacted or briquetted carbon black pigment granulate comprises: (a) mixing the pigment with one or more processing aids; (b) compacting or briquetting the mixture; (c) pulverising the product; (d) separating into two or more fractions; and (e) removing as final product the fraction with at least 85% of particles above 80 (especially above 100) mu m or with size 80-2,000 (especially 100-1,000) mu m and optionally rounding it, and discarding or recycling the other fraction(s).

Description

DK 176548 B1

The present invention relates to a process for preparing inorganic mold or briquette granules of inorganic pigments with adjuvants. These granules can be used in the dyeing of building materials such as concrete and asphalt and of organic media such as paint systems, molds and paint pastes. The processing of pigment granulates requires the grinding of the pigments into primary particles in order to obtain the optimal color impression. The powders thus formed are very strongly dusted, and because of their fine grain they tend ten! adhesion and adhesion in dosing systems. In the case of toxicologically hazardous substances, it is therefore necessary to take measures during processing. avoidance of danger to 10 people and environment due to the resulting sting. However, even with trouble-free inert substances such as iron oxide pigments on the part of consumers, there is an ever stronger desire to avoid dust pollution.

Therefore, the avoidance of dust and improved dosing due to better flow properties to obtain a qualitatively uniform color impression when used in building materials and organic media is the aim of handling pigments. This goal is achieved to a greater or lesser extent by the use of granulation processes on pigments.

In addition, structural or spray granulation is usually used. Compression methods have heretofore been less suitable because of the limited dispersibility of the granules thus formed. 20 In principle, pigment consumers require two properties which go in different directions, using pigment granulates: mechanical stability of the granulate and good dispersion properties. The mechanical stability ensures good transport properties, both during transport between manufacturer and consumer as well as good dosage and flowability in the use of the pigments. The mechanical stability is induced by high adhesive forces and depends, e.g. by the amount of binder or also by the pressing pressure during forming. On the other hand, the dispersibility is affected by a good grinding prior to the granulation (wet and dry milling), the mechanical energy of incorporation {shear forces} and dispersing aids which immediately reduce the adhesive forces in the dry granulate when incorporated into a medium.

However, for pigments, the use of larger amounts of dispersing aids is limited due to the cost / pigment cost ratio. Furthermore, a high addition ratio causes a corresponding decrease in color strength or spreading ability. Since the color strength variations are usually below ± 5%, the use of additives is also limited, even when they simultaneously act as adhesive formulations 35 and dispersant aid. Furthermore, the additives must not alter the use characteristics of the end products, such as e.g. building materials, plastics and lacquers, in an unfortunate manner, for example by the concrete strength or solidification forbidden, by the asphalt compressive strength or the tear strength, and by the plastics strength or notch strength, and by elastomers (polymers) the elastic properties, 5 for example, pigmenig granuates are used for spray granulation (spray drying over slab or nozzle) and buildup granulation (mixer, swirling flag granulator, plate or drum).

In spray drying granulation, pigment suspensions are used and binders are used. Such methods are described in various patents.

10 In these cases, water-soluble binders are used. Thus, DE-A 3 619 363, EP-A 0 268 645 and EP-A 0 365 046 are based on organic substances such as e.g. lignin sulfonates, formide hydrate condensates, gluconic acids, sulfated polyglyco ethers, while in accordance with DE-A 3 918 694 and US-A 5 215 583, inorganic salts are used, e.g. silicate and phosphate, EP-A 0 507 046 discloses a combination of spray granulation and structure granulation. ! DE-A 3 619 363 (spa 3, lines 44-47) and EP-A 0 268 645 (spa 7, lines 18, 19) are exempted from the use of a compression method. In this method, by applying pressure, a strong cohesion of the particles is obtained, so as to obtain good transport stability but at the same time also lower dispersion properties.

20 in EP-A 0 257 423 and DE-A 3 841 848, the syringe granulation is described using polyorganosiloxanes as hydrophobic, lipophilic additives. Said spray dryer usually leads to small particle sizes, i.e. high content of fine particles. This means that a substantial part of the material is not obtained as directly usable granulate from the dryer, but as fine particle land is first retained in the filter and then must be recycled in the process. The hydrophobic finishing of spray granulated products results in a granulate with extremely good flow properties, but which is extremely dusty.

EP-A-0 424 836 discloses the preparation of dust-poor finger granules in a workflow in known intensive mixers. A low content of wax is used here in combination with emulsifier and wetting agents when applying an aqueous dispersion.

This usually results in water content from 20 to over 50%. These granules must first be dried and isolated from the top and bottom grains.

DE-A 31 32 303 discloses dust-poor, rice-resistant inorganic pigment granules which are mixed with binder liquids which are liquefied under heat and granulated by a sigie process using sieve aid (pressure). Thus, approx. 10-20% of the passed material as fine particle proportion <0.1 mm.

EP-A 0 144 940 discloses dust-poor pigment granules which from filter sludge with approx. 50% water by the addition of 0.5-10% surfactants and another 5 mineral oil or waxes which are made liquid are mixed at 50-200 * 0 to the softening point. The process is carried out in intensive mixers and, if necessary, subsequent granulation and drying . In the final product, water is present in an amount of 10-15%, which is unfortunate for incorporation into resins.

EP 0 651 031 A1 discloses a method for dyeing organic media by means of inorganic pigment granules. These inorganic pigment granules are prepared by mixing one or more inorganic pigments with one or more adjuvants. The mixture is subjected to a pressing step and the pressed product is comminuted.

The comminuted product is upgraded.

Other methods also have limited utility. The spray granulation due to the droplet formation requires the use of light liquid, ie. thin liquid suspensions. Thus, in the drying process, a greater amount of water must be evaporated than in the frequently used fluidized bed swirl drying of high-pressure pigment paste pastes. This leads to higher energy costs. In the case of pigments which have been prepared in advance by spraying, spray granulation means a further 20 steps of high energy cost. Furthermore, with the spray granulation, a greater or lesser amount of the fine particulate material in the dust filter appears, and this material must be recycled in production.

The structural granulation often also has disadvantages. It can be carried out - based on pigment powder - in mixers under high turbulence, in the vortex layer method 25 or also by plate and irom granulation. Common to these processes is that the need for binder, mostly water, is high, so that as a subsequent process step a drying must be connected. Here, too, granules of varying sizes are obtained, especially when there is insufficient binder for the amount of powder available or the actual distribution is not optimal. Then a certain proportion may be too large as granules, while on the other hand too small and thus dusty proportions appear. It is therefore necessary to classify the granules formed with a reflux of upper and lower grains.

The tailer granulation leads to a wide particle size spectrum of granules. Where this is not desired due to the poor dispersibility of large particles, the granulation process must be followed by intensive personnel monitoring, and the production of granules should! is optimized by manual control of the seed rate. Usually a classification is also made here with return of upper ·· and sub-grains.

Extrusion procedures from pastes lead to drying by ten! granules which also because of their size do not ensure optima! dispersibility.

From DE-A 42 14 195 a method ten is known. dyeing asphalt with inorganic pigment granules, where as a binder! used oil. This is a simple granulation process.

In DE-A 4 336 613 and DE-A 4 336 612, inorganic pigment granules are prepared from pigments by mixing with binders, compression, crushing and granulating. These granules produced in this way are difficult to transport pneumatically and during transport a lot of dust is produced which is undesirable.

Therefore, it is the object of the present application to provide a method which avoids the hitherto described disadvantages of spray granulation, extrusion granulation or structure granulation in their application to 15 inorganic pigments and provides sufficiently stable dosed, dust-poor granules with preferably the same good dispersing capabilities as .

It has been found that this can be achieved by a multistage combination of the steps of mixing, compressing, isolating and optionally rounding.

The present invention relates to a process for producing inorganic mold or briquette granules of inorganic pigments with auxiliary agents, the process being characterized in that a) one or more inorganic pigments are mixed with one or more auxiliaries which promote processing ability, b) (c) the molded or briquetted product is comminuted; (d) the finely divided product is separated into two or more fractions by size; (e) the fraction in which at least 85% of the particles are greater than 80 µm, preferably greater than 100 μτη, or lying between 80 and 2,000 lutes, preferably between 100 and 1,000 µm, is withdrawn as a product and optionally rounded off in an additional step, 30 and the other fraction or fractions removed from the process or recycled.

Preferred embodiments of the method are set forth in claims 2-12. preferably, before step c), the pressed or briquetted product can be separated into two fractions by size {intermediate step x), followed by the coarse fraction in which at least 35% of the particles are greater than 500 µm. preferably 600 μηι, can be comminuted in step c), and the second fine fraction in step d) alone or together with the product of step c) again be paired into two or more fractions by size.

Preferably, only the fine fraction is separated from intermediate step x) into two or more fractions by size in step d), while the coarse fraction from intermediate step x) is decomposed at step 5 c} and then taken from the process as a product.

The intermediate step x may preferably be accomplished by sieving or sieving (mechanical separation). Preferably sieving machines are used.

It is particularly preferred to divide the liquid product in step d) into two fractions by size, as the fine particle fraction less than 80 µm is withdrawn or recycled in the process, and the coarse fraction greater than 80 µm is optionally rounded in an additional step.

The finely divided product may also preferably be divided into three fractions by size in step d), whereby the fine particle and coarse particle fraction is withdrawn from the process or recycled in the process, and the fraction is between 80 and 2,000 µm, most preferably between 100 and 1,000 µm, and most preferably between 100 and 100 µm. and 500 µm, optionally rounded off in a further step.

The granules preferably have a residual water content of less than 4% by weight, especially preferably less than 2% by weight. This may also be achieved by post-drying.

The rounding step under e) is preferably carried out while removing the dust part.

Preferably, the product obtained after step e) of the rounding process can be further coated with auxiliaries.

When completing a rounding step under e). advantageously, then, a coarse fraction of particle sizes> 1,500 µm may be isolated which may be recycled in the process.

Preferably, as inorganic pigments, iron oxide, titanium dioxide, chromium oxide, rollile phase phase pigments and mixtures of these pigments with soot pigments are used.

The inorganic pigment granules preferably have shaving serum weights between 0.5 and 4.0 g / cm 3, more preferably between 0.5 and 2.0 g / cm 3. The soot pigment blend granules preferably have shaking room weights of from 0.3 to 1.5 g / cm 3.

As auxiliaries can be used both inorganic and organic substances.

As auxiliaries, water, salts of the group of phosphates, carbonates, nitrates, sulfates, chlorides, silicates, aluminates and borates, form later, oxalates, citrates and tartrates, polysaccharides, cellulose derivatives such as e.g. cellulose ethers, cellulose esters, phosphonocarboxylic acids, modified silanes. silicone DK 178548 B1 6 animals, claimants of biological origin (eg rapeseed oil, soybean oil, maize germ oil, olive oil, coconut oil, sunflower oil), refined petroleum oils on paraffinic and / or naphthenic basis, synthetically produced oils, alkylpbenols, glycoplastics, polyglycoys, polyglycoio derivatives, protein fedic acid condensation products, acylbenzenesulfonates, alkyl naphthalene sulfonates, lignin sulfonate, sufated polyglyco ethers, melamine formaldehyde condensates, naphthalene formaide hydrocarbon condensates, giuconic acid, giuconic acid

Further, in the mixture, emulsifiers, wetting agents and dispersants may be used in an amount of 0.01 to 5% by weight, preferably 0.01 to 3% by weight, based on the weight of the pigments used. '

In particular, as emulsifiers, emulsifiers having HL6 values from 7 to 40, especially from 8 to 18, can be used for use in building materials with aqueous systems such as e.g. concrete consisting of alkyl, acrylic and hydrophilic intermediate and end groups, such as e.g. amides, amines, ethers, hydroxyl, carboxylate, sulfate, sulfonate, phosphate, amine salt, polyether, polyamide, polyphosphate. The substances can be used individually or in combination with their HLB value.

As wetting agents, especially alkylbenzene sulfonates, fatty alcohol sulfates, fatty alcohol benz sulfates, fatty alcohol ethoxylates, alkyl phenol ethoxylates, alkane, olefin sulfonates are suitable.

As dispersing aids, melamine sulfonates, naphthalene sulfonates, metal soaps, polyvinyl alcohols, polyvinyl sulfates, polyacrylamides, fatty acid sulfates are preferably used.

To increase the stability or to aid in the processing of the granules, it may be beneficial to eventually coat the granules with an additional layer. This layer may be formed by application of inorganic salts in solution, of polyols, oils or waxes or polyethers, polyarboxylates or cellulose derivatives. , preferably carboxymethyl cellulose.

The granules can also be further added to the mixture with preservatives at a concentration of 0.01 to 1% by weight, based on the weight of the pigment. As examples, formaide anhydrous compounds, phenolic compounds or isothiazolinone preparations may be mentioned.

Unsurprisingly, for the mold and briquette granules, especially when intended for sand working in aqueous building material systems, such as cement mortar! or concrete, not course is used in water-soluble substances as auxiliary, but also water-insoluble substances, such as e.g. oils.

DK 176546 B1 7

The auxiliaries are preferably used in amounts of 0.001 t 10% by weight, especially from 0.01 to 5% by weight, most preferably from 0.1 to 3% by weight, based on pigment used.

The auxiliaries may preferably be used in conjunction with additional additives such as e.g. emulsifiers, wetting agents, metal soaps, etc.

The briquetting press urine b) is preferably carried out on a wafer or matrix press and preferably at line forces of 0.1 to 50 kN / cm, preferably 0.1 to 20 kN / cm.

At pressing, the briquetting (compression, step b)) is an important characteristic of the compressive force (kN) per cm roller width (line force). The compression between rollers assumes a linear transfer of the pressing force, since no pressing surface can be determined and therefore no pressure (kN / cm2) can be calculated.

The compression is preferably carried out at low line forces. The line forces used are usually preferably in the lower range of the commercially available apparatus, preferably between 0.1 and 50 kN / cm. Very specific linear forces of 0.1-20 kN / cm are preferred. Commercial appliances are e.g. Pharmapaktor 200/50 from the company Bepex GmbH, Leingarten / Duitsiand.

The additional separation step x) is preferably carried out with sieving machines, such as e.g. drum screens, swing screens and vibration screens.

The comminution can be carried out with all commercially available comminution assemblies such as crushers, tooth rolling mills, rollers with friction devices and screen granulators.

The comminution step c) is preferably carried out with sieve granulators or with sieving furniture, by which the material is pressed through a pass sieve having a mesh of from 0.5 to 4 mm, especially preferably from 0.5 to 2.5 mm, particularly preferably from 1 to 2 mm (so-called “crusher). As known, the rotors move rotating or oscillating at a peripheral speed of 0.05 m / sec. to 10 m / sec, preferably 0.3-5 m / sec. The distance between the rotor and sieve or bulb is 0.1-15 mm, preferably 0.1-5 mm, especially preferably 1-2 mm.

For example, a flake crusher from Frewilf, Freiburg / Switzerland can be used as a finding device.

After the comminution, the fine particle portion under BO p, m was separated. Preferably, the amount of this fine particle fraction is 10-50% by weight, especially preferably 10-30% by weight. The fine particle portion is preferably recycled to step b). The residue is rice-resistant, OK 176546 B1 8 dosed, stable, dust-poor and with good dispersibility. A further optimization can be achieved by subsequent rounding.

The rounding step under e) is preferably carried out on a turntable, a rotary drum or drum ring drum, on drum generators or similar apparatus or in a rotary layer or in a seam. Here, the dust part can preferably be sucked off or removed in the bed-bed by means of luff.

The advantage of the process according to the invention lies, inter alia, in that dried or possibly ground pigment powder can be used as a starting material.

This is especially economical when the pigment is produced by calcination. For example, the spray granulation requires a renewed mixing and then a further drying step. In addition, it is very uneconomically economical to remove the water used in the mixing process by evaporation.

The process according to DE-A 43 36 613 or DE-A 43 38 612, due to the build-up granulation on the turntable, admittedly files round particles, which, however, are inhomogeneous. They consist of a compact core and one or more buildable outer layers that can be torn off. These products are therefore dusty especially in the pneumatic transport and the flowability is not very good. The products of the process according to the invention do not have these disadvantages, since they consist of homogeneous compact articles of uniform density and strength.

The granules prepared by the process according to the invention are used for dyeing building materials, e.g. concrete, cement mortar, plaster and asphalt, and for dyeing organic media such as lacquers, resins and color pastes, and for the production of dispersion paints and slurries.

The granules prepared by the process of the invention are particularly suitable for incorporation into dry cement mortar mixtures and in plaster.

In the four-step method of the present invention, it is essential that in the first step a sufficiently cohesive homogeneous material be formed by adding the auxiliary in a mixer, in the second step briquetting or pressing is then carried out.

For dyeing building materials such as concrete or asphalt with inorganic pigments, inorganic briquette or mold granules of inorganic pigments and auxiliaries prepared by the process of the invention are mixed with the building material in an amount of 0.1-10% by weight, preferably 1- 5% by weight, based on cement,

Granules prepared by the process of the invention can also advantageously be used in dispersion dyes and slurries.

DK 176548 B1 9

For dyeing organic media such as lacquer systems; plastics and color pastes with inorganic pigments; inorganic briquette or mold granules of inorganic pigments prepared by the process of the invention are blended with the organic medium in an amount of 0.1 to 10% by weight. calculated on organic medium.

Testing of the dispersibility of building materials is carried out in cement: mortar over the paint strength measurement on prisms made with white cement:

Cement quartz sand ratio 1: 4, water-cement value 0.35, pigmentation height 1.2%, based on cement, used mixer from RK Toni Technik, Berlin, with 5 10 l mixing shed, construction 1551, speed 140 ο / min. mixture: 500 g of cement.

After 100 s, 3 mixture samples (300 g) are taken and sample bodies (5x10 x 2.5 cm) are prepared under fryer (300 bar). Hardening of test bodies: 24 hours at 30 ° C and 95% relative humidity with subsequent drying for 4 hours at 6G ° C. Color data measurement via Dataflash 2000 Datacøior International, Cologne, 4 measuring points per stones, 12 measuring points 15 per, pigment admixture. The obtained average values are compared with the values for a reference sample. Assessment of the color distance EaG and the color strength (reference sample ™ 100%) (DIN 5033, DIN 8174). Dispersibility is considered good by a color strength difference of up to 5% over the reference sample, which is satisfactory by a research up to 10%.

The test of the dispersibility in asphalt is carried out as follows:

Pigment / pigment granules are mixed in a heated laboratory mixer (Rego mixer) with a roadway bitumen type B 80 (commercial product from Shell AG) and additives for 80 seconds at 180 ° C. With the mixture, test bodies are prepared according to Marshall ('The. Shell Bitumen Handbook, Shell Bitumen U.K., 1990, pp. 230-232). Far-25 vetone differences between the Marshmallows in relation to a given comparison sample are color-metric (Minolta Chromameter II, standard light type C, Cielab system. DIN 5033, DIN 8174) when comparing the red value a *. Differences in the a * ~ values below 0.5 units cannot be seen with the naked eye.

The flowability test is performed by assessing the outlet ratio 30 for a 100 ml volume with 8 mm opening in accordance with ASTM test D 1200-88. The flow ratio is termed as good when the material flows freely. If there is no material outflow or an outflow only after knocking, the flow ratio is considered insufficient.

Determination of the fine particle proportion as the screen man's is carried out on a 35 VA screen according to DIN 4188 with a mesh size of 80 gm on an air jet screening machine 10 DK 176548 81

type Alpine 200 IS, 20 g of sample material is used, the fine particulate matter is extracted over a period of 5 minutes and the amount of coarse particles on the sieve is weighed. The test of the plastic dispersibility is carried out in accordance with a regulation conforming to DIN 53 775, Part 7, “Prufung von Farbmitteln in weichmaeherhaitigen Polyvinylchloride (PVC-P) molding mass; Determination of Dispersion Hair by WalzenY

The pigment which is tested is dispersed at 160 t 5 ° G on a PVC rolling mill. The resulting roller skin is divided and half is then subjected to increased shear forces by rolling at room temperature. The color distance ΔΕ according to CIELAB (Din 5033, 6174) 10 between warm and cold-viscous PVC skin, or white pigments is the difference in the standard color value Y (DIN 5033) between hot »and cold-viscous PVG-color. skin. A good dispersible pigment is already dispersed at low shear forces, while ten! To disperse a highly dispersible pigment, the increased shear forces at the lower temperature rolling are required. Therefore, the smaller the color spacing 15 ΔΕ or the difference in the standard color value ΔΥ ers, the better the pigment is dispersible. Especially in granules, dispersibility is of great importance, since the granulate particles must first be comminuted before dispersing in the mold. For granules, an equally good dispersibility is sought as for the corresponding pigmeni powders, so that the characteristics ΔΕ or Y for powders and granules are not significantly different.

20 The fine dust measurement for assessing the strength of granules is carried out in accordance with DIN 55 992. The dusting properties of a granulate can be measured with a Heubach "Dustmeier", The removal of fine dust from a rotating drum through which an air flow of defined strength is determined gravimetrically For measurements after different loading times, the course of dust evolution as a function of mechanical impact can also be determined.

The present invention is further illustrated by the following Examples, COMPARATIVE EXAMPLE 1 30 kg of iron oxide red Sayferrox 130 (commercial product from Bayer AG) is mixed with 1% lignin sulfonate and 1% machine oil V 100 in a mixer for 10 minutes. The mixture is pressed on a compactor 200/50 (Fa. Bepex, Leingarten) with approx. 10 kN (2 kN / cm) and then comminuted on a crusher {Fa. Frevvitt, Friborg, Switzerland) with a screen width of 1.5 mm. The proportion above 80 µm is above about 95%. The dispersibility in 35 concrete, compared to the initial powder, is 100%. The shake room weight is 11 OK 176546 B1 1.07 g / crr \ The material is heavily dusted and does not run from a hopper with a 6 mm opening.

EXAMPLE 2 0.8 kg of the finely divided (see Example 1} and then sieved material (coarse water over a sieve with a mesh size of 300 µm) is rounded into a vortex layer. As apparatus is used a 90 mm diameter glass tube and a height of 665 mm with a glass-free G 0 as an air distributor, the filled-in amount (4% other than 80 µm) is swirled with an air flow of 22 NnrVb for 10 minutes or 30 minutes, The ripped 10 material is withdrawn with an air stream. or 30% of the material as a fine particle proportion. The dispersibility of the building material is well 95% or 94% relative to the strongness of the material. The material flows well. The dust dust (dust measurement with dust meter from Heubach in accordance with DIN 55 9S2) is very small, the shaking volume is larger than that of the starting material. 100% of the material is at a control sieve above 15 125 µm. The average particle size is at approx. 800 pm. The amount of particulate matter separated is 34% or 42%.

Example 3 1 kg of the material after comminution into the crusher (see Example 1) is added to a 20 drum sieve with a diameter of 220 mm and a length of 310 mm and with a mesh width of 300 µm at 10 rpm. minute (rpm), which is in a closed house. The house with a volume of approx. 35 S is extracted from above. After an operating time of 10 minutes or 30 minutes, 30% or 37% is suctioned. The material exhibits clear rounding, irregular shape, dispersibility and flow conditions are good.

25 The tendency for dust formation is low. Further rolling (rounding) on a turntable (diameter 40 cm, 42 rpm, 47% slope) causes no further improvement.

COMPARATIVE EXAMPLE 4

The material treated in the crusher (see Example 1} is rolled on the rotary screw (diameter 40 cm, 42 rpm, 47% slope) during extraction. The yield is 95%. The dispersibility is good. The material tightens well. The proportion over 80 pm is 100 However, the pupil ratio in the dust meter is very poor by about 300 mg The dust value for the granules from Examples 2 and 3 in the dust meter is, however, at about 100 mg, EXAMPLE 5 250 g of soda Corasol C30 (commercial product from Fa. Degussa) or 250 g of soot Monarch 800 (commercial product from Fa. Cabot Corp.) and 250 g of iron oxide variety Bayferrox 330 (commercial product of Bayer AG) are mixed with ammonium lignin sulfonate and machine oil V 100 in various quantities in a mixer for 18 minutes. The blend is pressed on a compact type WP50N (Company Alexanderwerk, Remscheid) with different line forces one to two times and then comminuted in a finger modulator RFG (Fa. Aiexanderwerk, Rernscheid) with a screen having a mesh width of 1.5 mm from 1 , 5 The ten-part product is separated over a sieve with a mesh width of 250 µm into two fractions. The fraction above 250 p.m is tested and shows a good flow capability (the corresponding starting powder mixture has a poor flow capability). The other data from the fraction purified from the starting powder are shown in Table 2. The relative color strength is measured in relation to a corresponding mixture of starting powders.

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Claims (12)

1. Method Ten! preparation of inorganic mold or briquette granules of inorganic pigments with auxiliary agents, characterized in that a) one or more inorganic pigments are mixed with one or more auxiliaries 5 which promote processing ability, b) the mixture is subjected to a pressing or briquetting step, c) the pressed or briquetted product is comminuted; (d) the comminuted product is separated into two or more fractions by size; (e) the fraction in which at least 85% of the particles is greater than 80 µm, preferably 10 greater than 100 µm, or is between 80 and 2,000 µm. , preferably between 100 and 1,000 µm, is taken out as a product and optionally rounded off in an additional step and the other fraction (s) removed from the process or recycled. Process according to claim 1, characterized in that before step c) the pressed or briquetted product from b) is divided into two fractions by size, the coarse fraction, in which at least 85% of the particles are larger than 500 µm, preferably larger than 800 µm, is added to step c) and comminuted, and the fine fraction is added ten! step d) to be divided into step d) separately or together with the product of step c). Process according to claim 1, characterized in that the finely divided pro-; (d) is subdivided into fractions according to size, where the fine portion of less than 80 20 µm is taken out or recycled in the process, and optionally the coarse fraction larger than 80 µm is rounded in a subsequent step. Process according to claim 1, characterized in that the finely divided product is divided into three fractions according to size in step d), the fine particle portion and the coarse particle portion being taken out or recycled, and optionally the middle fraction 25 is rounded off between 80 and 2,000 pm step. Process according to one or more of claims 1-4, characterized in that the rounding step under e) is carried out during removal of the dust part, Process according to one or more of Claims 1 to 5, characterized in that the product obtained according to step d) or optionally the product obtained after rounding in step e) 30 is coated with auxiliaries. Process according to one or more of claims 1 to 6, characterized in that, as inorganic pigments, iron oxide, titanium dioxide, chromium oxide, roti-phase phase pigments and mixtures of these pigments with soot pigments are used. Process according to one or more of claims 1-7, characterized in that water is used as an auxiliary, salts from the group of phosphates, silicas, afuminates, borates, polysaccharides and eellulose derivatives, oils of biological origin, refined paraffin and / or naphthenic base oils, synthetic synthetic oils, alkyl phenols, gycoes, polyethers. polyglycols, polyglycol derivatives, protein fatty acid condensation products, alkylbenzenesulfonates, acylnaphthalene sulfonates, lignin sulfonate, sulfated polyglycol ethers, melamformideide condensates, naphthalene-formaldehyde condensates, gluconic acid, gluconic acid, gluconic acid Method according to one or more of claims 1-8, characterized in that the auxiliaries are used in amounts from 0.001 to 10% by weight, based on the pigment used. Method according to one or more of claims 1-9, characterized in that the pressing or briquetting step b) is carried out on a wire press or die press and at line forces from 0.1 to 50 kW cm, preferably 0.1 to 20 kN / cm, Method according to one or more of Claims 1 to 10, characterized in that the finding step (c) is carried out by sieving over a passage screen having a mesh width of 0.5-4 mm, preferably 0.5-2.5 mm, especially preferably from 1 to 2 mm. Method according to one or more of claims 1 to 11, characterized in that the rounding step under e) is carried out on a turntable, S a turning drum, s a sieving system or in a web layer.