HK1040733A1 - Process for producing briquetted and pressed granular and use thereof - Google Patents

Description

Method for producing briquetted and pressed granular material and use thereof

This application is a divisional application of the patent application with application number 97111242.8.

The present invention relates to a process for producing briquetted and pressed granular material and its use for dyeing building materials such as concrete and asphalt, and organic media such as paints, plastics and mill bases.

To achieve the best color effect, the production of pigment particles requires grinding the pigment into elementary particles. The powder thus formed generates a large amount of dust which, because of its finely dispersed state, tends to adhere and stick to the dosing equipment. For toxic and harmful substances, protective measures must therefore be taken during the production process in order to avoid damage to humans and the environment due to the dust formed. However, even for safe inert substances such as iron oxide pigments, there is an increasing need in the market to avoid the irritation due to dust.

The aim of treating the pigments is therefore to avoid dust and to improve the dose as a result of good flowability, so that color effects of consistent quality are achieved when used in building materials and organic media. This object is achieved in principle by a process for granulating pigments. Granulation and spray granulation are generally used here. The compression-moulding process has hitherto not been very suitable, since the dispersibility of the granules obtained therewith is limited.

In principle, for the application of pigment particles, the market requires pigments with two diametrically opposed properties: mechanical stability and good dispersibility of the particulate material. Mechanical stability is the main cause of good transport properties during transport between the manufacturer and the user and good dosing and flowability of the pigment during use. It results from a high adhesion and depends, for example, on the amount of binder and even on the molding pressure during molding. On the other hand, dispersibility is affected by intensive grinding (wet grinding and dry grinding) before granulation, mechanical energy (shear force) during mixing, and dispersing agents, which directly reduce the adhesion between dry particulate matter during mixing into a medium. However, the use of large amounts of dispersants in pigments is limited due to the cost ratio of additives to pigments. In addition, a high proportion of additives will correspondingly reduce the color strength or the scattering power. Since the variation in the coloring strength is usually less than. + -. 5%, even an additive serving as both a thickener and a dispersant is limited in use. Furthermore, the additives must not adversely alter the use of the end products, such as building materials, plastics and coatings: for example, the strength or setting of concrete, the compressive strength or abrasion resistance of asphalt and the strength or notched impact resistance of plastics and the elasticity of elastomers (polymers).

According to the prior art, suitable production methods for pigment granules are: such as spray granulation (tray or nozzle spray drying) and granulation (mixer, fluidized bed granulator, tray or drum).

Spray drying granulation starts from the pigment suspension by using a binder. Related methods are described in the various claims which are protected; wherein a water-soluble binder is used. The processes in DE-A3619363, EP-A0268645 and EP-A0365046 start from organic substances, such as lignosulphonates, formaldehyde condensates, gluconic acid, polyethylene glycol ether sulphates, while the processes in DE-A3918694 and US-A5215583 start from inorganic salts, such as silicates and phosphates. A combination of spray granulation and granulation is described in EP-A0507046. DE-A3619363 (column 3, lines 44-47) and EP-A0268645 (column 7, lines 18, 19) employ compression moulding. In this process, strong adhesion of the particles is achieved with pressure, so that good transport stability can be achieved, but at the same time the dispersibility is reduced.

Spray granulation with polysiloxanes as hydrophobic, lipophilic additives is described in EP-A0257423 and DE-A3841848. The spray dryers mentioned generally result in small particle sizes, i.e. a high proportion of fine material. This means that an effective proportion of the substances cannot be made directly available as granular substances by the dryer, but they are first left in the filter as fine substances and then have to be returned to the process. For spray-dried products, post-treatment to render the material hydrophobic will produce a granular material with very good flowability, but dust is particularly severe.

EP-A0424896 describes the production of low-dust fine particulate material, the production operation being carried out in known intensive mixers. A low level of wax is mixed with an emulsifier and a wetting agent to produce an aqueous dispersion. Water contents of from 20% up to more than 50% are generally obtained in this process. These granular materials must first be dried and separated from the materials with the over and under particle sizes.

DE-A3132303 describes fine-flowing and low-dusting inorganic pigment granules which are mixed with a binder which becomes liquid under the action of heat and granulated by sieving with a sieving device (pressure). About 10-20% of the flow rate is accumulated as fine material < 0.1 mm.

EP-A0144940 describes low-dusting pigment granules, starting from a filter deposit containing about 50% water, which are mixed until the lubricating point is reached by adding 0.5 to 10% of a surfactant and a wax or mineral oil which liquefies at 50 to 200 ℃. The production is carried out in an intensive mixer, if necessary granulating and drying the mixture. The final product contains 10-15% water, which is disadvantageous for incorporation into plastics.

Other methods are also limited in their application. Spray granulation requires the use of a well-flowing and well-liquefied suspension due to the formation of small droplets. Therefore, for this drying process, a larger amount of water has to be evaporated than in the conventionally available fluidized-bed drying process from the high-pressure filtered pigment slurry, which results in high energy consumption. For pigments previously produced by calcination, spray granulation involves an additional, energy-intensive treatment step. In addition, during spray granulation, a greater or lesser proportion of fine material accumulates and must be returned to the production facility.

Granulation also often shows disadvantages. Starting from pigment powders, the process can be carried out in a fluidized-bed process in a mixer under high turbulence conditions, or by pan granulation and drum granulation. Common to all these processes is that the amount of binder (in most cases water) required is so high that an additional process step of drying is necessary subsequently. Here, also granular substances of different sizes are obtained, especially if the binder is insufficient or the actual distribution is not optimal for a certain amount of powder. For use as a granular substance, some fraction may be too large, while on the other hand some fraction is too small, so that dust formation still exists. The resulting granular material must be sorted to return both oversized and undersized material.

Pan granulation produces granular particles with a wide range of particle sizes. This is undesirable because too large particles have poor dispersibility, the granulation process must be controlled by manual, intensive manipulation, and the production of granular materials must be optimized by manually controlling a large number of particles. Usually after which sorting will also take place and return of the over-and under-sized material.

During the drying process, the extrusion process starting from the slurry results in the formation of a relatively solidified granular mass; due to their particle size, they do not guarantee optimum dispersibility.

DE-A4214195 describes a process for dyeing bitumen with inorganic pigment granules using oil as binder. The process is a simple granulation process.

In ED-A4336613 and DE-A4336612, inorganic pigment particles are produced by mixing a pigment with a binder, press-molding, coarse grinding and granulating. The granular material thus obtained is not satisfactorily conveyed by wind power plants; during transport, a large amount of dust is formed, which is undesirable.

It is therefore an object of the present invention to provide a process which makes it possible to avoid the disadvantages of spray granulation, extrusion granulation or granulation described hitherto in the application thereof to inorganic pigments and which makes it possible to provide sufficiently stable, dosable granular materials which have low dust content and are equally well dispersible as the powders used hitherto.

It has now been found that this object can be achieved by a combination of a plurality of steps of mixing, pressing and separating, possibly in addition to a rounding step.

The invention provides a process for producing briquetted and pressed granular material from inorganic pigments and auxiliaries, which process is characterized in that: a) mixing one or more inorganic pigments with one or more processing-enhancing auxiliaries, b) subjecting the mixture to a pressing or briquetting step, c) comminuting the product obtained by the pressing or briquetting, d) dividing the comminuted product into two or more parts, e) removing that part of at least 85% of the particles which is larger than 80 μm, preferably larger than 100 μm, or which is between 80 and 2000 μm, preferably between 100 and 1000 μm, and possibly rounding it in an additional step, while the other part is diverted from the process or returned.

Before step c), the pressed or briquetted product can preferably be divided into two parts (intermediate step x) in order then to break up the coarse fraction in step c), in which at least 85% of the particles are larger than 500 μm, preferably 600 μm, and to separate out the other fractions, and to divide the fine fraction into two or more parts again in step d), which are separated from or put together with the product from step c).

Preferably, in step d), only the fine fraction obtained in the intermediate step x) is divided into two or more parts, while the coarse fraction obtained in the intermediate step x) is comminuted in step c) and the process is then transferred out as product.

The intermediate step x) can preferably be carried out by pneumatic separation or sieving (mechanical separation). Preferably a sieving device is used.

It is particularly preferred that in step d) the comminuted product is divided into two portions, the fine fraction smaller than 80 μm being transferred out of or back into the process, while the coarse fraction larger than 80 μm can be rounded off in an additional step.

It is also possible to divide the comminuted product into three portions in step d), to transfer the fine and coarse portions out of the process or back into the process, while the intermediate portion between 80 and 2000 μm, particularly preferably between 100 and 1000 μm, most preferably between 100 and 500 μm, can be rounded off in an additional step.

The granulated material preferably contains residual water in an amount of less than 4% by weight, particularly preferably less than 2% by weight. This can be achieved by post-drying if necessary.

e) The rounding step in (4) is preferably carried out with removal of the dust portion.

Furthermore, the product formed by rounding in e) can preferably be coated with auxiliaries.

If the rounding step in e) is carried out, the coarse fraction with a particle size of > 1500 μm can be separated off later and returned to the process.

The inorganic pigments used are preferably iron oxide, titanium dioxide, chromium oxide, rutile mixed-phase pigments and mixtures of these pigments with carbon black.

The inorganic pigment particles preferably have a bulk density of 0.5 to 4.0g/cm³In particular between 0.5 and 2.0g/cm³In the meantime. The bulk density of the particles mixed with carbon black is preferably 0.3 to 1.5g/cm³。

Both inorganic and organic substances can be used as auxiliaries.

The auxiliaries used are preferably water, salts selected from phosphates, carbonates, nitrates, sulfates, chlorides, silicates, aluminates and borates, formates, oxalates, citrates and tartrates; polysaccharides, cellulose derivatives such as cellulose ethers, cellulose esters, phosphonocarboxylic acids, modified silanes, silicone oils, biologically cultivated oils (e.g. rapeseed oil, soybean oil, corn oil, olive oil, coconut oil, sunflower oil), refined petroleum oils based on paraffins and/or naphthenes, synthetic oils, alkylphenols, glycols, polyethers, polyethylene glycols, polyethylene glycol derivatives, protein fatty acid condensates, alkylbenzenesulfonates, alkylnaphthalenesulfonates, lignosulfonates, polyethylene glycol ether sulfates, melamine formaldehyde condensates, naphthaldehyde condensates, gluconic acids, polyhydroxy compounds or aqueous solutions thereof.

In addition, emulsifiers, wetting agents and dispersants may preferably be added in amounts of from 0.01 to 5% by weight, preferably from 0.01 to 3% by weight, based on the weight of the pigment used, during the mixing process.

For use in aqueous building material systems, such as concrete, suitable emulsifiers are, in particular, emulsifiers having an HLB value of from 7 to 40, especially from 8 to 18, which consist of alkyl or acryloyl groups and hydrophilic middle parts and end groups, such as amides, amines, ethers, hydroxyl groups, carboxylic acid esters, sulfates, sulfonates, phosphates, amine salts, polyethers, polyamides, polyphosphates. These may be used individually or in combination according to their HLB value.

Suitable wetting agents are, in particular, alkylbenzenesulfonates, fatty alcohol sulfates, fatty alcohol ether sulfates, fatty alcohol ethoxylates, alkylphenol ethoxylates, alkylsulfonates, olefinsulfonates.

Melamine sulfonates, naphthalene sulfonates, metal soaps, polyvinyl alcohols, polyvinyl polysulfates, polyacrylamides, fatty acid sulfates are preferably used as dispersants.

In order to increase the stability of the granular material or to facilitate the production of the granular material, it is advantageous to coat the granular material with an additional layer last. The layer can be prepared by applying an inorganic salt solution, a polyol, an oil or wax or a polyether, a polycarboxylate or a cellulose derivative, preferably carboxymethyl cellulose.

Preservatives may also be added to the granular material during mixing, in concentrations of from 0.01 to 1% by weight based on the weight of the pigment. Examples which may be mentioned are compounds which release formaldehyde, phenolic compounds or isothiazolinone formulations.

Surprisingly, the aids for compacting and briquetting particulate matter (especially if they are to be used as added to aqueous building material systems such as cement mortars or concretes) can be not only water-soluble substances but also water-insoluble substances such as oils.

The auxiliaries are preferably added in an amount of from 0.001 to 10% by weight, particularly preferably from 0.01 to 5% by weight, most preferably from 0.1 to 3% by weight, based on the pigment used.

The auxiliaries which can be added are preferably substances which are compounded with further additives, for example wetting agents, metal soaps, etc.

The pressing or briquetting step b) is preferably carried out using a roll press or a mould press, preferably at a line pressure of from 0.1 to 50kN/cm, preferably from 0.1 to 20 kN/cm.

In pressing or briquetting (press forming, step b)), an important value is the pressure per cm of roll width (kN) (line pressure). During the compression between the rolls, the pressure is considered to be transmitted linearly, since the surface on which the pressure is applied cannot be determined and therefore the pressure (kN/cm) cannot be calculated²)。

The press forming is preferably performed under a low line pressure. The line pressure applied is generally preferred in the lower range of commercially available equipment; preferably between 0.1 and 50 kN/cm. The line pressure is most preferably 0.1 to 20 kN/cm. An example of a commercially available device is the Pharmapaktor 200/50 manufactured by Bepex GmbH (Leingarten/Germany).

The additional separation step x) is preferably carried out with screening machines such as rotary screens, vibrating screens and oscillating screens.

The comminution can be carried out by all industrial comminution apparatuses, for example crushers, toothed-roller crushers, roller mills equipped with friction apparatuses and screen mills.

The comminution step c) is preferably carried out with a screen crusher or screen mill, in which the material is pressed through a screen (so-called crusher) having a screen opening of 0.5 to 4mm, particularly preferably 0.5 to 2.5mm, most preferably 1 to 2 mm. As is generally known, the movement of the impeller is cyclic or oscillating, with a peripheral speed of 0.05 m/s to 10 m/s, preferably 0.3 to 5 m/sec. The distance between the impeller and the screen or crusher toggle plate is 0.1-15mm, preferably 0.1-5mm, most preferably 1-2 mm.

An example of a comminution apparatus which can be used is the Flake crusher manufactured by Frowitt (Fribourg/Switzcrland).

After grinding, the fine material smaller than 80 μm is separated. The amount of the fine substance is preferably 10 to 50% by weight, particularly preferably 10 to 30% by weight. Preferably, the fine material is returned to step b). The rest part has good flowing property, can be used for dosing, has low dust and is easy to disperse. In addition, the best results are achieved by an additional rounding step.

The rounding step e) is preferably carried out on a rotating disk, in a drum or a pull-cord drum, in a drum screen or the like or on a fluidized bed and in a screening apparatus. The dust fraction can here preferably be removed by suction or conveyed away by air over a fluidized bed.

One advantage of the process according to the invention is that it is possible to start with dried and ground (if necessary) pigment powder. This is particularly economical when the pigment is produced by calcination. For spray granulation, for example, further slurrying and an additional drying step thereafter are necessary. In addition, the process is very expensive, since it takes into account that evaporating off the water used for slurrying would consume energy.

According to the processes in DE-A4336613 or DE-A4336612, it is possible to round off inhomogeneous granules by granulation on a rotating disk. They consist of a dense core and an outer layer or a layer formed thereon, which can be ground off. These products therefore form dust, especially when conveyed by compressed air, and are particularly poorly flowable. The products obtained by the process according to the invention do not have these disadvantages, since they consist of homogeneous, dense granules with uniform density and strength.

The granular material produced according to the process of the present invention can be used for dyeing building materials such as concrete, cement mortar and plaster, also for dyeing organic media such as paints, plastics and pigment pastes, and also for producing disperse dyes and slurries.

The granular material produced according to the invention is particularly suitable for incorporation into dry cement mortars, and into plasters.

In the multistage process of the invention, it is important that a homogeneous mass of sufficient viscosity is prepared in the first stage by adding auxiliaries in a mixer. Then briquetted or pressed in a second step.

The invention also provides a process for dyeing building materials, such as concrete or asphalt, with inorganic pigments, characterized in that a compacted or pressed inorganic granular material is made of inorganic pigments and auxiliaries and is produced by the process of the invention, the granular material being admixed with the building material in an amount of from 0.1 to 10% by weight, preferably from 1 to 5% by weight, of the cement.

Another preferred use of the particulate material produced according to the present invention is in disperse dyes and slurries.

The invention also provides a process for dyeing organic media, such as coating systems, plastics and pigment pastes, with inorganic pigments, characterized in that briquetted or pressed inorganic particulate material is made of inorganic pigments and produced by the process of the invention, the particulate material being mixed with the organic medium in an amount of from 0.1 to 10% by weight of the organic medium.

The dispersibility in the building materials in cement mortars was tested by measuring the colour strength according to the spectrum generated by the white cement according to the following method:

the cement-quartz sand ratio is 1: 4; the water-cement ratio is 0.35; the pigment deposition degree is 1.2% of the cement; the mixer used, with a 5-liter mixing cylinder, is available from RK Toni Technik, Berlin, construction type 1551, with a rotational speed of 140 rpm; 500g of cement as a raw material required for one operation. After 100 seconds, test pieces (5X 10X 2.5cm) were prepared under pressure (300 bar) using 3 samples of the mixture (300 g). Curing of the test block: at 30 ℃ and 95% atmospheric humidity for 24 hours and then at 60 ℃ for 4 hours. Color data were measured according to Dataflash 2000, Datacolor International, Cologne, at 4 points per stone and 12 points per pigment blend. The obtained average value was compared with the value of the standard sample. Color difference Eab and tinting strength (standard = 100%) (DIN5033, DIN6174) were evaluated. The difference in the coloring strength from the standard sample was up to 5%, and the dispersibility was said to be good, and the difference was satisfactory up to 10%.

The dispersibility in bitumen was tested according to the following method: the pigment/granular pigment was mixed with road asphalt type B80 (commercial product manufactured by Shell AG) and the aggregate in a heatable laboratory mixer (Rego mixer) at 180 ℃ for 60 seconds. Test blocks were prepared from this mixture using The Marshall method ("The Shell Bitumenhandbook, Shell Bitumen U.K.,1990, pages 230-. The difference in hue of the Marshall test block with the predetermined reference sample (Minolta C hromameter II, standard lizumab C, Cielab System, DIN5033, DIN6174) was evaluated colorimetrically by comparison of the red value a. a difference of less than 0.5 units is not easily perceived by the naked eye.

Flowability was tested by evaluating flow from a 100ml funnel with a 6mm opening according to ASTM Test D1200-88. If the material is free flowing, the flowability is considered good. Poor flow is considered if the material does not flow, or flows only after removal of the plug.

The fines were determined (due to the oversize openings) with an Alpine 200LS type air-jet classifier according to DIN 4188 on a VA sieve with openings of 80 μm. The test was carried out with 20g of sample. The fine material was removed by suction for 5 minutes and the coarse fraction on the sieve was reweighed.

According to DIN53775, section 7 "Testing of cementitious immobilized polyvinyl chloride (PVC-P) materials; determination of the dispersibility of the plastics in the determination of the dispersion of the dispersing hardness by two roll milling "experiments.

The pigments tested were dispersed in PVC at 160. + -. 5 ℃ using a mixing roller. The resulting rolled layer was separated and then half exposed to increase shear force by rolling at room temperature. The measure of dispersibility is the color difference Δ E of CIELAB (DIN5033,6174) between the PVC layers with hot and cold rolling for the color pigments, and the difference of the standard tristimulus value Y (DIN 5033) between the PVC layers with hot and cold rolling for the white pigments. Easily dispersible pigments can be dispersed even at low shear, while increasing shear during low temperature rolling is required to disperse relatively less easily dispersible pigments. The law is therefore: the smaller the difference in color difference Δ E or standard tristimulus value Y, the better the dispersibility of the pigment. Dispersibility is very important, especially for particulate matter, since the particles of particulate matter dispersed in the plastic material must first be separated. For granular materials, dispersibility as good as that of the corresponding pigment powder is sought so that the characteristic values Δ E or Y of the powder and the granular material do not differ too much.

The fine dust particles used to determine the stability of the particles were determined in accordance with DIN 55992. The particle formation dust can be determined with a Heubach "dust tester". The amount of fine dust particles emerging from the drum can be determined gravimetrically by passing a stream of air of a specific density through a glass fibre filter. By performing the measurements after varying the exposure period, the improvement in dust formation can be determined, due to the effect of mechanical stress.

The present invention will be described in more detail with reference to the following examples, which should not be construed as limiting the invention thereto.

Example 1 (comparative)

50kg of iron oxide red Bayferrox 130 (a commercial product from Bayer AG) was mixed with 1% lignosulfonate and 1% V100 motor oil in a mixer for 10 minutes. The mixture was pressed in an 200/50 compactor (firm Bepex, Leingerten) with a force of about 10kN (2kN/cm) and then comminuted in a crusher (firm Frewitt, Fribourg, Switzerland) with a sieve having a mesh opening of 1.5 mm. The proportion of more than 80 μm is about 95%. The dispersibility in concrete compared with the starting powder was 100%. The bulk density was 1.07g/cm³. The material formed a large amount of dust and did not flow out of the funnel with a 6mm opening.

Example 2

0.6kg of the coarsely ground (see example 1) and subsequently sieved material (coarse fraction after passing through a sieve having a mesh size of 300 μm) was rounded in a fluidized bed. The apparatus used was a glass tube 90mm in diameter and 665mm in height and fitted with a frit glass filter G0 as an air inlet. With 22Nm³The amount of air/h was vortexed for 10 min and 30 min for the amount added (4% of the fractions were less than 80 μm), respectively. The abraded material is discharged by an air stream. The amounts discharged as fine material were 20% and 30%, respectively. The dispersibility in cement mortar was good in the case of relative color strengths of 95% and 94%, respectively. The fluidity of the material was good. The dust rate is very low (dust determination according to DIN55992 using a Heubach dust tester) and the bulk density is greater than that of the starting material. 100% of the material was greater than 125 μm as shown by the control sieve. The average particle size was about 600. mu.m. The amount of fines separated was 34% and 42%, respectively. Example 3

1kg of the material comminuted by the disintegrator (see example 1) was placed in a trommel screen of diameter 220mm, length 310mm and mesh size 300 μm, which was operated at 10 revolutions per minute (10 revolutions per minute), which was placed in a closed hood. Suction was applied to the top of the hood, and the volume of the hood was about 35 liters. After 10 and 30 minutes respectively, 30% and 37% were aspirated. Irregularly shaped material is significantly rounded. The dispersibility and the flowability were both good. The tendency to form dust is small. Further rolling (after rounding) on a rotating disk (diameter 40cm,42 revolutions per minute, angle of inclination of 47 degrees) did not bring about any further improvement.

Example 4 (comparative)

The coarsely ground material (see example 1) was then rolled by post-rolling on a rotating disk (diameter 40cm,42 rpm, 47 degrees angle of inclination) for 15 minutes under suction. The yield was 95%. The dispersibility is good. The material flow was good. The proportion of more than 80 μm is 100%. However, the indication of dust formation on the dust meter was about 300mg, very poor. In contrast, the dust values on the dust meter of the granular materials obtained in examples 2 and 3 were about 100 mg.

Example 5

250g of Corasol C30 carbon black (commercial Degussa) and 250g of Monarch800 carbon black (commercial Cabot Corp), respectively, were mixed with 250g of Bayferrox330 black iron oxide (commercial Baye AG) in a mixer for 18 minutes with varying amounts of ammonium lignosulfonate and V100 motor oil. The mixture was pressed once or twice with different line pressures in a WP50N type compactor (manufactured by Alexanderwerk of remischeid), and then pulverized in an RFG fine mill (manufactured by Alexanderwerk of remischeid) with a sieve having a mesh size of 1.5 mm. The pulverized product was divided into two parts by using a sieve having a mesh opening of 250 μm. The test was carried out with a fraction greater than 250 μm, which showed good flowability (the corresponding powder mixture had poor flowability). The remaining data relating to this fraction and the original powder are shown in table 2. The relative colour strength was determined and compared with the corresponding original powder mixture. TABLE 1

Sample (I)	Annotation of samples	Yield [% ]	Dispersibility of	Measured dust [ mg ]	Time of flow [ sec ]	Bulk density [ g/cm3〕	Sieving analysis is more than 80 μm
								Example 1	Pressing and pulverizing	100	100	-	No flow	1.07	95
Example 2	Sieving: in a fluidized bed for 10 minutes	66	95	104	32	1.14	100
								Sieving: in a fluidized bed for 30 minutes	58	94	85	32	1.17	100
	Example 3	Sieving for 10 minutes by a rotary drum sieve	70	96	95	32	1.10								100
Sieving for 30 minutes by a rotary drum sieve								63	94	71	30	1.11	100
		Passing through a rotating simple sieve for 10 minutes and rolling on a rotating disc for 15 minutes	70	95	96	30	1.11							100
Example 4								Without sieving, roller compaction on a rotating disk for 15 minutes	95	98	304	29	1.22		100

In cement mortar; relative color intensity [% ]Table 2

	Additive agent	Line pressure [ kN/cm ]	Bulk density [ g/ml ]	Yield [% ]	Time of flow [ sec ]	Relative colour strength in concrete [% ]
							Monarch800 carbon Black powder	--	--	0.20	--	Can not flow	100
Bayferrox 330: Monarch 80050: 50; granules	2% LS + 1% oil	7	0.6	61	34	83
							Corasl C30 carbon black powder	--	--	0.40	--	Can not flow	100
Bayferrox: Corasol 50: 50; granules	8% LS + 1% oil	5	0.6	54	31	96
							Bayferrox330 iron oxide powder	--	--	0.7	--	Can not flow	100

LS = ammonium lignosulfonate oil = V100 motor oil

Claims (3)

1. A method for dyeing building materials including concrete, cement mortar and plaster with granular substances made of inorganic pigments and auxiliaries by briquetting and pressing, and for dyeing organic media including paints, plastics and pigment pastes, and for producing disperse dyes and slurries.

2. A method of dyeing building materials, which comprises mixing briquettes and pressed granular material produced from inorganic pigments and auxiliaries with the building materials in an amount of 0.1-10% by weight of the cement.

3. A process for dyeing organic media, which process comprises mixing briquettes and pressed granular material produced from inorganic pigments and auxiliaries with the organic media in an amount of from 0.1 to 10% by weight of the organic media.