DE1421258B1 - Process for the production of shaped coke from coals of any kind - Google Patents

Description

a) the rapid heating of the coal in an oxygen-containing atmosphere at temperatures at which though expelled moisture, but no significant amounts are formed at Teerdämpfen that amount at non-caking coals 120 to 260 ° C, wherein caking coals, however, 260-430 ⁰ C. , for a period of 5 minutes to 3 hours, the oxygen content in the treatment of non-baking coals being 1 to 8%, in the case of baking coals 8 to 20%,

b) the rapid heating of this coal to a higher temperature not exceeding 650 ° C, this temperature is maintained for 10 to 60 minutes,

c) the further rapid heating of this coal to temperatures between 760 and 980 ^° C., this temperature being maintained for at least 7 minutes until the reactive coke now present has a volatile content of no more than 3 percent by weight, based on a moisture and ashless substance,

d) the subsequent cooling of the reactive coke to a temperature between 16 and 33 ° C above the softening point of the binder subsequently added for briquetting using a cooling gas practically free _{of CO 2} , steam and O _2,

e) mixing the reactive coke with a bituminous binder,

fj the briquetting of the mixture at a pressure of more than 350 kg / cm,

45

g) curing the briquettes in an atmosphere containing 2.5 to 21 percent by volume of O ₂ at 230 to 260 ° C for a period of 90 to 180 minutes,

h) the subsequent coking of the moldings at temperatures above 815 ° C and

i) cooling the moldings to about 260 ⁰ C.

55

The invention relates to a method for producing molded coke from coals of any type, according to the the coal is gradually heated, partially oxidized and degassed in the fluidized bed, whereupon the so pretreated coal is mixed with a binder, briquetted and coked.

Conventional coke, which has long been the main source of carbon in iron making and others metallurgical operations is becoming increasingly expensive and difficult to obtain because the appropriate ones Coking coal stores are used up.

Attempts have now been made to store coal at low temperatures, i.e. H. at temperatures from 420 to 650 ° C, to degas and thus obtain a carbonaceous material for the production of molded coke. These However, degassing processes resulted in a brittle coke material that cannot be used to produce Form coke was suitable, which can be used as a substitute for blast furnace coke. So much for these procedures Having been used on a large scale, they were used to produce liquid and gaseous distillates used, which had a relatively low content of aromatics. The waste product was above all suitable for the production of fuel.

It has been proposed to handle finely divided coal particles in the fluidized bed. A fluidized bed coking, as previously done, results in a porous, weak, and friable char product low density unsuitable for metallurgical use in briquette form. At low Coal products produced in the fluidized bed and at high temperatures have very rugged exteriors Surfaces, with little of the original structure of the coal particle being preserved. In contrast in addition, they have the typical, open-pore structure of conventional coal products.

The briquetting of coal particles by degassing processes at low or high temperatures (including fluidized bed processes) were produced in a previously known manner, resulted in inhomogeneous Products. This lack of homogeneity manifested itself in the fact that it was within the structure of the briquette the original individual coal particles can be determined with the microscope, which are stuck together by coke, which arises from the binding material. There are two types of coke side by side, which have different properties, so that the briquette for metallurgical Purposes is unsuitable. Experience shows that the coke formed from the binder with different and reacts faster than the coal coke, so that the briquette becomes the original dissolves fine coke particles. The particles are withdrawn from the process without reacting to have been used, so that there are economic disadvantages and technical difficulties.

The previously known shaped coke is suitable as fuel and for other purposes, but not for metallurgical purposes Processes like iron smelting. The previously known molded coke is insufficient Strength to be able to withstand the conditions in a blast furnace and can therefore not be used as metallurgical carbon.

In detail, the following processes to be mentioned in the present context have become known so far.

- From the magazine »Glückauf« 92 (1956), issue 11/12, P. 327, left column, paragraph 2, and right column, paragraph 1, is a procedure of the type specified above basically known. Without further details being given, a procedure is mentioned in this journal described in the highly volatile coal by treatment with highly heated gases at gradual with increasing temperature in the fluidized bed partially oxidized and then degassed so far that they no longer bake, i.e. practically all volatile components have been driven out of the coal. Afterward is known as' Pech briket-

animal and smoldering or coked. More details however, are not specified.

From U.S. Patents 2131,702 and 2030 852 as well as British Patent 785 863 are various methods of treating To take coal. U.S. Patent 2,030,852 describes a process for converting bituminous Coal in coke. The coal is heat treated in three stages. It is a common one Coking process.

US Pat. No. 2,131,702 describes a method for coking a coking coal in which Coarse coal or preferably briquetted coal, made by grinding the coal and through Briquetting made with a binder is heated in a number of stages. This Process requires the use of a charcoal suitable for coking.

From British patent 785 863 a method for treating coal with a oxygen-containing gas can be taken.

Processes for producing briquettes from coke are known in principle from the magazine "Bergakademie" 1958, Issue 1, Μ pp. 19 to 25, and US Pat. No. 2,869,992.

A three-stage heating process for coals is also known from British patent specification 175 888, in which, however, relatively large pieces of coal of a certain kind in thin layers during a be heated for a longer period of time.

Finally, there is a comparable one from the published German patent application St 3626, however two-stage process can be found.

The invention is based on the object of a method for treating coal of any type (in particular cheap and generally available coal that is of no coke quality) through the a solid, chemically reactive, carbonaceous material can be produced that is called metallurgical Carbon can be used in briquette form.

According to the invention, this object is achieved by a method of the type described at the outset, which is characterized by the following, essentially known measures:

a) the rapid heating of the coal to be formed, however, no substantial amounts of Teerdämpfen in an oxygen containing atmosphere at temperatures at which though expelled moisture amount at non-caking coals 120 to 260 ⁰ C, in caking coals, however, 260 to 43o ⁰ C , for a period of 5 minutes to 3 hours, the oxygen content in the treatment of non-baking coals being 1 to 8%, in the case of baking coals 8 to 20%,

b) the rapid heating of these coals to a higher ^{temperature not exceeding 650 °} C., this temperature being maintained for 10 to 60 minutes,

c) the further rapid heating of these coals to temperatures between 760 and 980 ⁰ C, this temperature being maintained for at least 7 minutes until the reactive coke now present has a volatile content of no more than 3 percent by weight, based on a moisture and ashless substance,

d) the subsequent cooling of the reactive coke to a temperature between 16 and 33 ° C above the softening point of the binder subsequently added for briquetting using a cooling gas practically free _{of CO 2} , steam and O _2,

e) mixing the reactive coke with a bituminous binder,

f) briquetting the mixture at a pressure of more than 350 kg / cm ² ,

g) curing the briquettes in an atmosphere containing 2.5 to 21 percent by volume of O ₂ at 230 to 260 ° C for a period of 90 to 180 minutes,

h) the subsequent coking of the moldings

Temperatures above 815 ° C and i) cooling the moldings to about 260 ° C.

In this context, reactive coke is a coke that arises after it has gone through stages a) to c) Understood coke material, which is chemically reactive in a special way to be explained later and therefore enables the production of solid, non-friable briquettes.

The resulting product is remarkably strong, abrasion resistant, homogeneous and extremely uniform in reaction with carbon dioxide, steam and oxygen. It forms extremely strong carbon-carbon bonds with the carbon developed from tar and pitch, which is obtained in the production of the coke material, or with coal tar or other bituminous binders, so that a stronger, internal, three-dimensional connection to the production of molds with high dimensional stability and the resulting briquettes for metallurgical purposes are ideally suited.

The moldings are hardened (stage g) at a temperature below the coking temperature of the bituminous binder, with the temperature, however, for copolymerization of the binder with the coke particles is sufficient. The hardened bricks are coked. To avoid losses is done coking preferably in an atmosphere free of carbon dioxide, water vapor and oxygen is.

The following describes the lignite, non-coking coals with a high proportion of volatile components, coking coals and anthracites preferred applicable process conditions are shown.

Grind

The coal, if not already finely divided, is made by any known milling process crushed until essentially all of the particles pass through a 2.4 mm mesh (No. 8 mesh) sieve and 95% will be held through a 0.044 mm mesh (325 mesh) screen, with a minimum There is a quantity of fine particles of a size which escape from the cyclone of the fluidized bed reactor would. This is generally achieved by milling in a hammer mill.

1st heating stage (a)

The finely ground coal particles are initially - preferably in a fluidized bed, but alternatively in a disperse phase - subjected to a pretreatment, due to which the formation of peroxides and hydroperoxides is promoted. These substances

act as catalysts in the formation of a coke material that is free from bubbles, cracks and others Faults and is not brittle. This is preferably done in an oxygen-containing atmosphere, whose Concentration in inverse proportion to the oxygen concentration of the coal being treated fluctuates. The practical range used is 1 to 20 percent by volume in the incoming flow agent (Steam or gas), depending on the type of coal. For low-grade, non-coking coal, an oxygen concentration is used near the lower limit of this range, for example from 1 to 8 percent by volume, used; for coking coals, an oxygen concentration in the upper part of this range, for example from 8 to 20 percent by volume, used. The oxygen concentration should be the maximum Represent the amount of oxygen that goes into the carbon matrix and thus a source of oxygen during the Process step forms and prevents agglomeration without uncontrolled combustion in this first heating stage or in later stages. For coals with a high oxygen content the oxygen can be derived from the coal itself, and the superplasticizer can be oxygen-free be.

In this heating the fluidized bed generally at a temperature of 120 to 260 ⁰ C is maintained at nichtkokenden coals including lignites. For baking and coking coals, a temperature of 260 to 430 ° C is chosen so that the unfavorable influence of these properties can be eliminated. The upper value of this range is the temperature point at which hydrocarbon vapors are produced. The lower limit is required so that the moisture content can be reduced to 2% or less, or, in the case of the coal with less than 2% moisture, so that oxygen can be added to the carbon matrix.

In carrying out this reaction, the starting coal is preferably continuously converted into a Brought fluidized bed, which is kept at the desired temperature, the heating being practical instantaneously, d. H. for a second or less.

The coal particles should be in the fluidized bed for at least 5 minutes, preferably 5 minutes to 3 hours remain. A response from 10 minutes to 180 minutes can be carried out without damaging the end product. The temperature is inversely related to the residence time.

The flow medium, preferably steam or exhaust gas, mixed with air or oxygen, is at a Pressure from 0.14 to 2.11 atmospheres at a speed initiated, at which the desired fluidized bed conditions occur, d. H. at a speed of 0.15 to 0.6m / sec. upon entry of the gas from the fluidized bed grid in the fluidized bed reactor.

The coal particles can be heated in the fluidized bed by burning a small part of the coal will. This is done by heating the fluidized bed medium or by indirect heat exchange.

Instead of carrying out this reaction in a fluidized bed, the finely divided carbon particles can also be heated in a disperse phase, ie dispersed in a suitable gaseous medium (e.g. in oxygen-containing exhaust gas, nitrogen or carbon dioxide within the limits indicated above) has sufficient velocity to keep the particles more in the disperse phase than in the dense phase, such as in a fluidized bed. When heated in the disperse phase, non-coking coals are heated to a temperature of 177 to 400 ° C for about 3 seconds. Coking coals are heated to 400 to 54O ^{0 C for about 3 seconds.}

2nd heating stage (b)

The coal particles obtained according to the first heating stage are carbonized in this stage or carbonized by subjecting them to a further heat treatment in a fluidized bed, wherein the amount of heat required by burning a limited amount of coal or that from it generated hydrocarbon vapors. This combustion is controlled by that only the amount of oxygen necessary to achieve the desired temperature is added. This Oxygen is supplied to the bed in the form of air as part of the fluidized bed medium, with the remainder Steam, nitrogen, exhaust gas, carbon dioxide, carbon monoxide, or any gas that does not interact with that can be Coal at this stage reacts. Alternatively, heat can again be supplied from the outside through a heat exchanger will.

At this stage the heating can be controlled so that either the carbon product as such receives optimal properties or that the amount of tar required as a binder is generated, or finally, that the maximum possible amount of tar arises, which in the case of anthracite or others Coals with a low content of volatile components, however, are not sufficient as a binding agent. The optimal conditions for each type of coal must be determined in the laboratory.

The temperature and residence time are critical. The lower temperature limit is determined by the temperature at which the activated coal develops tar-forming vapors in large quantities. This temperature is the same as that which forms the upper limit of the first heating stage described above, ie for coking coals 43O ⁰ C and for non-coking coals 260 ° C.

The upper limit is determined by the temperature above which the expanding coal particles form cracks, fractures and bubbles to such an extent that no size and shape regression of the original coal particle can occur. This upper temperature limit is about 620-650 ⁰ C. The higher the temperature is, the greater in general, the amount of tar generated.

The fluidized bed gas should enter the fluidized bed at a temperature that is not significantly below the temperature of the fluidized bed and not more than 11 ° C above that temperature. At lower temperatures, a considerable amount of coal or hydrocarbon vapors must be burned in order to generate the necessary heat to adapt to the bed temperature; this reduces the yield. If the temperature is more than H ⁰ C above the bed temperature, the product will not become uniform.

The fluidized bed medium enters at a rate such that the fluidized bed conditions desired occur, in general at 0.15 to 0.6 m / sec., and expediently at pressures of

about 0.14 to 2.1 atmospheres, preferably 0.35 atmospheres, the one Allow the process to be carried out evenly.

The material is kept in the fluidized bed at the aforementioned temperature for 10 to 60 minutes. Within these limits, changing the residence time enables the chemical reactivity to be regulated of the end product.

In the case of coals with a lower value than that of anthracite, a sufficient amount of binder is required formed for the production of moldings. In contrast, this is not the case with anthracite. By the second In the heating stage or carbonization stage, the anthracite is partially degassed and its structure is changed and thus prepared for the further stages of the process.

The second heating stage can be the continuation of a batch-operated first heating stage form, the particles treated by the first stage initially over the desired residence time have been kept at the required temperature and the temperature of the bed suddenly increases until the temperatures are reached by reaction of the oxygen content of the fluidized bed medium with the bed the second heating stage are reached. However, the process is preferably carried out continuously, by passing the product of the previous stage directly into a fluidized bed, which is at the temperature the second heating stage (carbonation or charring stage) is located. In this case are the heat transfer rates in the fluidized bed are so high that the particles are practically shock-wise be heated.

If the starting coal particles are not those described in the previous first heating stage After treatment, an irreversible expansion of the particles occurs in the form of breakage and bursting the pore walls. The resulting product can be used as heating material, however, it is unsuitable for the further process stages. Compliance with the previously described Conditions is therefore an important prerequisite for achieving the homogeneous, stable moldings of the present proceedings.

Extraction and production of the tar types

The portion emerging from the coal as gas and steam can be used to extract tar. This is done with the help of suitable condensation processes. The tar can, for example, by blowing up to a water content of 0.5% are dehydrated and thereby reach the desired viscosity (softening point according to ASTM Ring and Ball Test 38-107 ⁰ C, preferably 54-66 ⁰ C). The blowing medium used can preferably be air, and possibly also steam.

3rd heating stage (c)

In the third heating stage (calcination stage) the carbon product is heated further so that the amount of volatile, combustible substances in the end product is reduced to below 3%. This is expediently carried out in a fluidized bed at temperatures between 760 and 820 ° C. and a residence time of 7 to 60 minutes. One can even higher temperatures, but not more than about 980 ⁰ C, apply. When working in the range from 815 to 980 ^° C., residence times over 10 minutes reduce the chemical reactivity of the product, which is proportional to the length of the residence time over 10 minutes. A secondary effect of this heating process is the increase in the mechanical strength of the product.

The selected residence time offers the possibility of influencing the properties of the end product and is also dependent on the temperature. At the lower temperature, sufficient residence time is required to reduce the proportion of volatile, flammable substances to 3%. The lower limit of the residence time is practically 10 minutes ^{at 760 to 815 °} C. and should not be less than 7 minutes ^{even at 980 ° C.}

The fluidized bed atmosphere should not contain reactive gases, e.g. B. carbon dioxide or water vapor, contain. Oxygen is only permitted in an amount as it is with regard to the required heat input by oxidation of the coal. This oxygen is generally the air taken, which is added to the otherwise chemically inert fluidized bed medium. The concentration of air for this purpose, the inlet gas should not exceed 70%.

In addition, the fluidized bed medium can contain carbon monoxide, hydrogen, nitrogen and exhaust gas, whereby carbon dioxide and water were reduced to carbon monoxide and hydrogen by removing the exhaust gas previously z. B. was passed over a bed of hot carbon. The fluidized bed medium should be below Pressures are introduced that allow a smooth process. 0 to 2.1 atmospheres, preferably about 0.14 atmospheres are suitable. The speed must be used to create fluidized bed conditions sufficient and should preferably 0.15 to 0.6 m / sec. be.

It is advantageous to introduce the fluidized bed medium at around the working temperature of the bed, since lower temperatures an increased oxidation of the carbon product and thus an unfavorable effect of water vapor and carbon dioxide on the end product.

The heating can again be carried out in batches as a continuation of the first and second heating stages same fluidized bed can be done by bringing the fluidized bed temperature to the temperature range of the third Increase the heating level and hold the bed in this area until the process is complete. Preferably, however, the hot product of the second heating stage is directly in the fluidized bed of the Third heating stage introduced, which is already at the temperature of the third stage. In this Trap, the heat transfer rate is so great that the heating of the coal is practically intermittent he follows.

In this case, too, it should be mentioned that the desired product will not be produced unless the conditions are met of the aforementioned levels are observed. Otherwise a loose, brittle product will result with a very low bulk density, in which the structure of the starting coal is unfavorably and irreversibly changed. On the other hand, remain with the product of previous stages the structure and the bulk density of the starting coal practically preserved.

Cooling (d)

The subsequent cooling takes place quickly and immediately, resulting in a loss of responsiveness

209539/51

can be avoided. One or more fluidized beds are preferably used for cooling, in which the fluidized bed medium serves as a cooling medium, the heat transfer rate is so great that the cooling takes place instantaneously. Suitable cooling media are exhaust gas, nitrogen or Carbon monoxide introduced at a temperature that allows cooling and with a Speed that creates the necessary fluidized bed conditions. The speed can be in essentially the same as in the second and third heating stages. Cooling media, the essential Containing amounts of oxygen, water vapor or carbon dioxide are unsuitable as in terms of unfavorable influences occur on the high reactivity of the product.

For the production of the briquettes from the reactive coke product that is now available, cooling is carried out this to a temperature of 16 to 33 ° C, preferably about 28 ° C above the softening point of the bituminous binder used in the pressing process, and leads the molding process without exposing the product to air, as it is pyrophoric.

Mixing (e) (f)

After cooling the product of the third heating stage to the temperatures mentioned this is mixed with a suitable binder. The mixing ratio is preferably 75 to 90% coke material to 25 to 10% binder, based on the weight of the mixture.

Compliance with these limits is important, and not only with regard to the copolymerization the final briquettes with the desired strength, but also with regard to the required mechanical strength of the green compacts (uncured Moldings). Below the lower limit of the proportion of binder, the green compacts tend to fall apart. Above the upper limit, they soften when they harden and bake together, so that Losses and procedural difficulties occur. The optimal ratio is determined in the laboratory.

The mixing time is expediently such that the coke particles have a uniform layer of binder can be wrapped. However, the time is not particularly critical.

Preferred binders are coal tar pitch or pitch formed by the condensation of tar from the Gases is generated, which arise during the second heating stage.

To form green compacts from this coke-binder mixture, a compression pressure of over 350 kg / cm ^{2 is} advantageous. Below this pressure, the green compacts become crumbly and tend to disintegrate, so that the strength properties of the end product are not sufficient either. The maximum pressure that can be used depends on the size of the green compacts and the type of device used. In general, the higher the pressure, the greater the compressive strength of the briquettes.

The deformation to green compacts can be done in a conventional briquetting or pelletizing device Production of briquettes or pellets of the desired size can be carried out. The briquetting device may have molds or rollers that apply the pressure. An extrusion device can also be used, whereby the strand can be cut into bars of any length. In addition, there are surface tension pelleting devices into consideration. The size and shape of the green compacts is determined by the end use. For phosphorus reduction in usual For example, arc furnace, the preferred size of a molded cushion is about 1.8 1.5 χ 1.3 cm. For blast furnaces, the size is about 5 χ 2.5 cm. For cupola cushions from 15 χ 10 cm can be used.

Hardening (g)

The green compacts produced in this way are pyrophoric and unstable and cannot be stored in heaps will. They are therefore fed to the curing stage in which the copolymerization is promoted and maintained by heating the green compacts in an atmosphere containing 2.5 to 21% oxygen. This atmosphere can be created by using 100% air at low temperatures and low Bed heights are used or by the air with gases (e.g. carbon monoxide, nitrogen, exhaust gas, which contains little or no water vapor, ^ or carbon dioxide) is diluted compared to the Green compacts and the volatile, hydrocarbonaceous components of the practically not converted part of the binder are inert.

This copolymerization is carried out practically at the maximum reaction temperature that is compatible with the amount and type of binder, but below the ignition point of the volatile, hydrocarbon-containing components of the binder, which can be present in combustible concentrations outside the green compacts. The temperature must not exceed 28 ° C below the coke point of the binder, which is determined by ASTM as the point at which the coke begins to show up on the wall of the still. Baking of the binder must be avoided because the amount of binder that forms coke on curing directly reduces the amount of copolymerization of binder and coke product. These copolymers form the homogeneous starting material for the chemically uniform, mechanically strong coke M briquettes of the present invention. ™

The hardening time is 90 to 180 minutes, preferably about 120 minutes at the maximum temperature, ie, 230 to 260 ⁰ C. The curing conditions depend on the oxygen concentration in the curing atmosphere, the temperature, the thickness or height of the layer of the green compacts and the speed , with which the heat is supplied and removed. The oxygen acts as a catalyst in this stage. If the green compacts are heated at temperatures above the softening point of the unreacted binder in an oxygen concentration below 2.5%, the green compacts disintegrate very quickly. On the other hand, at temperatures close to the decomposition temperature of the binder and at layer heights of the green compacts over 60 cm, the volatile constituents of the binder will burn if the oxygen concentration exceeds 4% of the supplied hardening atmosphere. Therefore, the oxygen concentration should be kept below 4% under these conditions. In the case of layers of lower height, the oxygen concentration can be increased accordingly. For layers of 15 cm or less

20% oxygen (air) can be used in the curing medium.

The catalytic effect of the oxygen can, if desired, be achieved by adding other catalysts be promoted. Such catalysts can be incorporated into the green compact before curing. This can be gaseous, in solution or in solid form when mixing, or gaseous or in solution in the Curing atmosphere take place. Suitable catalysts are boron trifluoride and its complexes, aluminum chloride, Hydrogen peroxide, phosphoric acid etc. The amount of catalyst used can be 0.1 to 5%, based on the weight of the green compact. For example, maximum strength is obtained with Boron trifluoride complexes and aluminum chloride with a curing time of about 60 minutes. With hydrogen peroxide or phosphoric acid, maximum strength of the briquettes results after a curing time of 90 minutes.

The throughput speed of the hardening atmosphere, which is passed through the position of the green compacts, depends on the shape of the reaction vessel. With an inner diameter of 22.5 cm and a layer height of A throughput of 1681 / sec was found to be 1.2 to 1.4 m. as satisfactory.

The hardened bricks are pyrophoric and may therefore only be stored in an environment that excludes spontaneous ignition.

Coking (h) (i)

The cured moldings are coked at temperatures and times at which the volatile, combustible components are reduced to below 2%. This increases the strength and the desired reactivity of the end product at the same time. The temperature is generally above 815 ° C, the time at least 5 minutes, and the atmosphere is practically free of carbon dioxide, water vapor and oxygen. A minimum of 15 minutes is required at 815 ° C. At 930 ^° C., a minimum time of 10 minutes is required. At 815 ° C., coking can be carried out for about 1 hour without loss of reactivity. At 930 ^° C., coking is possible for about 40 minutes without a loss of reactivity.

The effect of the higher temperature is to increase the breaking strength and reduce the chemical reactivity. The effects can also be achieved by increasing the residence time at a certain temperature. Temperatures above 950 ^° C. are used when a product with low reactivity is desired. At high temperatures, such as about 2200 ⁰ C, with a residence time of about 90 minutes, a product with high strength but low chemical reactivity is obtained, which is used for construction purposes, such as for tubes and containers for the chemical industry and for cathode housings in cells for the reduction of aluminous ores to the metal is suitable.
Exhaust gas, which has been passed through a glowing carbon bed to reduce the carbon dioxide content to below 10 percent by volume, is a suitable medium for supplying the heat of coking to the molds. Hydrogen, carbon monoxide, nitrogen, hydrocarbon gases and the tar-free gases generated in the roasting oven can also be used for this purpose.

The stage leads to coke formation from the copolymer of binder and reactive coke product in the hardened molding, with a chemically and physically homogeneous carbon structure in the end product is produced.

The coking can take place, for example, in a vertical shaft furnace in which the hardened Briquettes, following the force of gravity, move against the hot rising gases.

The coked briquettes are cooled to a temperature (about 260 ^° C.) at which they can be exposed to the air without damage, if desired to a lower temperature. The cooling process can consist in that a cooling gas is passed over or through the layer of coked moldings. This cooling gas must be practically free of carbon dioxide, water vapor and oxygen. It is expediently introduced in the lower part of the shaft furnace, in the upper part of which the cured moldings are coked. The finished briquettes withstand breaking pressures of at least 210 kg / cm ² , remain stable under all processing and storage conditions, are extremely abrasion-resistant and show other favorable properties. If the aforementioned conditions are adhered to, briquettes with the desired chemical reactivity, which react uniformly and are extremely suitable for metallurgical furnaces, such as e.g. B. Blowing and phosphor furnaces are.

The following examples serve to further illustrate the invention.

Examples

In all examples, the coal was crushed in a hammer mill, producing coal particles all of which passed through a 1.2 mm mesh screen (Tyler 14) while 95% was held in a 0.044 mm mesh screen (Tyler 325).

Example 1 relates to a sub-bituminous coal, Example 2 relates to a non-coking, bituminous coal, Example 3 a slightly coking, bituminous coal, example 4 lignite and example 5 anthracite. The properties These coals can be seen in detail from the following table I.

Table I.

example 1 Example 2 analysis Example 4 Example 5 2690 3390 Example 3 2710 Calorific value (kcal) 18th 2.6 3430 25.2 4.2 Moisture (weight percent) 4th Volatile substance, based on 42.7 42.1 49.8 4.5 Dry matter (weight percent) 36.9 Bound carbon, based on 53.2 ■ 48.4 34.8 79.5 Dry matter (weight percent) 54

continuation

14th

Example 1 'Example 2

Analysis example 3

Example 4 Example 5

Ash, based on dry matter (percent by weight)

Elemental analysis, based on dry matter (percent by weight)

carbon

hydrogen

oxygen

nitrogen

sulfur

ash

4.1

70.8
5.2

18.8
0.9
0.8
3.4

6.9

72.9 5.6

13.97 0.63 0.48 6.42

9.7

73.3 4.96 9.53 1.37 2.20 8.64

15.4

61.3 4.41

16.98 1.25 1.99

14.07

11.8

The following Table II shows the process conditions for the various treatment stages.

Table II example 1 Example 2 Example 3 Example 4 Example 5

1st heating stage

Test duration (h)

Total solids charge (kg) Inner diameter of the treatment vessel (cm)

Temperature of the fluidized bed ( ⁰ C) dwell time (min)

Fluidized bed medium

Entry speed (m / sec)

Composition (volume percentage)

oxygen

nitrogen

Steam

2nd heating stage

Test duration (h)

Total solids charge (kg) Inner diameter of the treatment vessel (cm)

Temperature of the fluidized bed ( ⁰ C) dwell time (min)

Fluidized bed medium

Entry speed (m / sec)

Composition (volume percentage)

oxygen

nitrogen

Steam

3rd heating stage

Test duration (h)

Total solids charge (kg) Inner diameter of the treatment vessel (cm)

Temperature of the fluidized bed ( ⁰ C) .. dwell time (min) ...

87
3880

25.4
189

25th

0.26

2.0

7.0

91.0

87
3320

25.4
466
53

0.27

5.0
19.0
76.0

87
2090

34.5
810
21

10 26.2

7.64 177 26

0.15

1.1 40.4 58.5

11.5 12.2

7.64 438 46

0.21

3.2 49.5 47.3

5.5 8.6

7.64 877 16

13.4 17.0

7.64 316
44

0.24

1.4 38
60.6

9.3 8.8

7.64 454
32

0.34

4.2 45.2 50.6

6.6 6.0

7.64,899
37

10 24.4

7.64 177 36

0.12

1.2 36.2 62.6

11 13.8

7.64 510 61

0.20

5.2 58 36.8

7 8.16

7.64 871 62

3.8 177 20

0.12

1.5 98.5

3.8 482 20

0.12

3.2 96.8

3.8 900 20

continuation

example 1 Example 2 Example 3 Example 4 Example 5

Fluidized bed medium

Entry speed (m / sec)

Composition (volume percentage)

oxygen

nitrogen

cooling

Temperature of the fluidized bed ( ⁰ C) ..

Composition of the fluidized bed medium (volume percentage)

Fluidized bed medium temperature ( ⁰ C)

Mix
Type of binder

Amount of binder, based on

on the overall mix

(Weight percent)

Amount of coal product based on the total mixture

(Weight percent)

Mixture temperature ( ⁰ C)

Mixing time (min)

Molding process
Shape type

Pressure (kg / cm ² )

Size of the green compacts (outer
Diameter height) (cm)

Hardening

Bed height (cm)

Curing atmosphere temperature ( ⁰ C)

Composition of the curing atmosphere (volume percentage)

oxygen

Inert gas

Residence time of the bricks (min)

Coking

Bed height (cm)

Coking atmosphere temperature ( ⁰ C)

Dwell time (min)

Composition of the coking atmosphere (volume percentage)

Steam

CO ₂

Hydrocarbon

nitrogen

Coke yield

Based on the dry substance of the coal (percent by weight)

0.16

11.0
89.0

204
N (100%)

27

0.34

11.2
88.8

66

N (100%)
27

0.27

9.7
90.3

66
N (100%)

27

0.21

11.1
88.9

N (100%)

Tar of the 2nd heating stage blown through,
60 ⁰ C softening point

18th

82

71

Pillow briquettes
1410

0.95-1.9-1.27

213
± 11

3.5
96.5
120

183

920
10

18.2
4.1
9.5

68.2

58

20th

80
71
10

Extrusion
1410
2.86 x 1.9

1.9

± 5.6

21

79

120

1.9

927
10

5
95

58

18th

82
71
10

Extrusion
1410
2.86 x 1.9

1.9

± 5.6

21

79

120

1.9

927
10

5
95

65.2

80
71
10

Extrusion 1410
2.86 x 1.9

1.9

232 ± 11

120

1.9

927
10

5
95

0.13

100

93 N (100%)

Coal tar pitch, 60 ⁰ C

15th

85 70 10

Briquettes 1400 2.8 x 1.9

1.9 260 ± 5.6

21

79

120

1.9

927 10

5 95

85

209 539/51

17th

The following table III lists the physical and chemical properties essential for the end product Properties of the coals of Examples 1 to 5 and the corresponding properties of a commercially available comparison coal compared to each other.

Table III

attempt

example 1 Example 2 Example 3 Example 4 Example 5

Commercial metallurgical coke

SSG ... SD .... TI .... FB .... HM ... R

SAN .. SAW .. AD ...

R-CO ₂ RH ₂ O

FM ...

C.

S.

O ₂ .... ashes. QH ... H _e / C _a .

Physical Properties

1,000 1.010 1.007 1.030 10 58 Chemical Analysis 2.3 2.8 2.5 1.294 1.002 0.63 0.61 -0.67 0.61 -0.67 0.63-0.70 26th 54 85.8 83.70 74 0.78-0.86 0.40 95 95-98 90-95 90-93 0.85 0.72 0.80 95-98 65 266 278 244 211 1.17 1.05 0.77 485 70.3 5-3 / 4 5-3 / 4 5-3 / 4 5 0.52 1.52 2.29 6th 5-1 / 2 10 " ¹ MT ¹ ίο- ¹ ΙΟ " ¹ 0.53 1.27 0.08 ΙΟ " ¹ ίο- ² Microphysical properties 11.13 11.47 22.06 357 100.9 116.3 92.5 1.2 70 0.119 0.105 0.131 9 1.98 1.90 31 9.8 2 55 14.7 5.3 2.4 2.4 1.5 86.60 86.60 84.4 0.92 Chemical reactivity 0.92 0.2 0.87 28.7 0.87 0.6 0.50 29.6 0.50 1 0.18 0.18 0.5 10.93 10.93 13.3 94.1 94.1 422 0.127 0.127 0.028

In the table means

SSG is the apparent specific weight at 15.5 ° C, calculated from the weight and dimensions of the coked moldings, SD is the bulk density in g / cm ³ , determined according to ASTM-D-291,

TI the tumbler index according to ASTM-D-441, FB the breaking strength in kg / cm ² , determined on the basis of the surface pressure at which a cylinder with the dimensions 2.86 χ 1.9 cm broke, HM the Mohs hardness,

R is the electrical resistivity in O / cm ² / cm measured using a standard bridge using a test piece with a cross section of 1 cm ² and a length of 1 cm, SAN is the surface area obtained by the standard Brunner method , Emmet and TeI-1 er was determined using nitrogen as the absorbed gas, SAW the surface area determined by the same method using water vapor as the adsorbed medium, AD the absolute density determined according to the helium sorption method,

R-CO _{2 is} the reactivity in carbon dioxide, which was determined on the basis of the amount of coke that passed through a sieve with 0.59 mm mesh size (Tyler 28) and which in one hour in a carbon dioxide stream at 900 ° C and a throughput of 400 ml / min was consumed,

RH ₂ O is the reactivity in steam, measured by the amount of coke of the same size that was consumed in one hour in a steam stream at 825 ° C. and a throughput of 133 ml / min.

In the case of the two reactivity tests mentioned, the samples were first flushed free by argon with a throughput of 370 ml / min. Each sample was crushed and sieved. Particles were used which passed through a 0.84 mm mesh screen (US Standard 20) but were captured by a screen with about 0.55 mm mesh (US Standard 30).
The chemical analysis was carried out according to the method that has been published in the Bureau of Mines Bulletin No. 492, under the title "Methods of Analyzing Coal and Coke" by AC F ie 1 d η er and WA S e 1 ν ig.

FM the volatile constituents, C / H the weight ratio of carbon and Hydrogen,

HjC _a atomic ratio of hydrogen to carbon.

The above products and the usual comparative coke were microscopically 50 and 100 fold Examined magnification. All of the products made by the process of the present invention had open, contiguous pores, while the pores in conventional coke are open, but not were coherent. Those produced by the process according to the invention according to Examples 1 to 5 Coke products were homogeneous in appearance and there was no difference in the magnification mentioned detectable between the binder and the coke formed from the coal. The homogeneity of the product according to Example 5 was slightly lower. In the case of the comparative coke, however, was the product not uniform.

The chemical reactivity in air was tested by placing a coke molding over a bunsen flame was kept, the propane and air burned in such a proportion that the blue cone 7 cm long and ended ί cm below the coke molding to be tested. In any case, they were Products according to Examples 1 to 5 were evenly consumed and did not splinter. The hut coke on the other hand burned unevenly.

To further illustrate the invention, Table IV shows the physical and chemical Properties of the coke product of the third heating stage, which is responsible for the favorable properties of the Essential final product is those of four commercially available carbonaceous Materials (A to D) juxtaposed that are representative of the known amorphous, carbonaceous Materials can be viewed.

In this table, the abbreviations have the meanings mentioned above.

The real density is to be understood as the density that is obtained according to the usual water displacement method is determined.

Helium density is the apparent helium displacement, measured according to the standard procedure for helium displacement.
The helium solution ratio is understood to mean the ratio of the helium density to the actual density. This ratio gives an indication of the nature of the intermolecular structure of carbon. The higher the ratio, the more helium and other gases are absorbed by the carbon.

The X-ray diffraction gives the values for the interplanar distance (rf distance at 002 index) again. This value gives the distance between the molecular units or layers as they go through determines the scattering of X-rays from a source with constant flux and constant frequency because the jet sweeps the powdery sample with an angular range of approximately 180 °.

The orientation index factor is the ratio

from I _p to I _b , where I _{p is} the uncorrected peak intensity

sity of the 002 region of the X-ray diffraction and /; which indicates the interpolated background intensity at the same d- value.

P means pyrophoric, NP non-pyrophoric. The air flammability is determined by using a mass 45.6 cm in diameter and 91.5 cm high is placed in a closed container. If the mass changes by reacting with the air trapped in the container when the If the temperature of the mass above 120 to 150 ° C spontaneously ignites, the material is considered to be air-flammable, i.e. H. pyrophoric, classified.

The products according to 1 to 4 have an average particle size of 2 to 3 · 10 ⁶ Å.

Table IV

Physical Properties

Physical Properties

SSG

Surface SAN

real density (g / cm ³ )

Helium density (g / cm ³ )

Helium solution ratio ..
X-ray diffraction (Ä) ..
Orientation index factor
Hardness Mohs scale

Chemical reactivity

Air flammability

CO ₂ reactivity
H ₂ O reactivity

Proximity analysis moisture and ashless basis (weight percent

FM

Fixed C

1.20 282 1.78 2.97 1.67 3.82 1.80 6

31 46

2.0 98.00

0.700 60 1.75 2.52 1.44 3.85 1.55 6

21

27

2.50 97.50 0.770
213
1.85
3.78
2.04
3.77
1.51
6th

15th
25th

2.50
97.50

1.12
401
1.97
3.28
1.66
3.71
1.33
6th

70.4
67

3.00
97.00

1.25

1.90
1.90
1.00

6th
NP

0.5
99.5

1.00
23.7
1.74
2.18
0.8
3.51
3.03
6th

NP

2.4
2.8

0.5
99.5

1.00

6.0

1.86

1.94

0.96

NP
1.6
2.0

0.1
99.9

1.30

0.8

1.66

1.83

0.91

3.56

4.07

NP

2.5
3.0

0.2
99.8

continuation

Physical Properties

Final analysis of moisture and
ash-free base (weight percent)

C.

H ₂

N ₂

S.

O ₂ by difference

HJC _a

C / H

Ash content moisture-free base
ash

95.10
1.35
1.33
0.46
1.76
0.170

71

5.82

95.01 1.38 1.56 0.49 1.56 0.174

69

11.76 95.75

1.11
1.42
0.53
1.19
0.139
86

13.09

96.00
1.20
1.28
0.58
0.94
0.150

80

23.18.

98.68
0.58
0.11
0.52
0.11
0.071
170

5.80

95.58
0.75
1.30
1.33
1.04
0.094

127

10.52

96.50
0.46
0.92
0.62
1.50
0.057
210

5.41

It should be noted that the coke product obtained after the third heating stage is a real one Has a density of 1.75 (2) to 1.97 (4), while the comparison products have real densities of 1.83 to 2.19 have. The products manufactured according to the invention have a hydrogen content of 1.11 (3) to 1.38 (2), which is much greater than the hydrogen content of the comparative products (0.46 to 0.75), and a carbon / hydrogen ratio from 69 (2) to 86 (3), which is considerably lower than the corresponding ratio of the comparison products is (127 to 210).

It can also be seen that the product according to the invention has an orientation index factor within a range from 1.2 to 2.8, while the comparable value of the comparison material is 3.03 or 4.7. The material according to the invention therefore has a significantly lower degree of order for the carbon crystals. The helium solution ratio in the product according to the invention is about 1.3, in the case of the known products, on the other hand, at 1 or below.

That is, the product according to the invention is considerably higher for helium and other gases Has absorption capacity than the comparative product.

The CO ₂ reactivity of the product according to the invention is at least 10%, whereas it is in the range from 1 to 2.4 for the comparative product. This increase in reactivity is in the range of five times. The hydrogen vapor reactivity of the product according to the invention is 25 to 67, that of the known products is 2 to 3.5%.

These considerably higher reactivity values confirm the low Orientation Index value; H., that the product according to the invention has changed less into the graphite state and therefore chemically is more reactive than the comparable products. In addition, the product according to the invention reacts uniformly with carbon dioxide and water vapor and also differs from the in this respect well-known products.

In further experiments, which are not given in detail, the temperatures and curing times were changed, while the other conditions remained unchanged. It was found that at temperatures over 950 ⁰ C, ie approximately at 1370 to 2200 ° C, and a sufficiently long, in inverse proportion to the temperature standing time products were obtained with a smaller chemical reactivity and a higher strength was found.

Claims (1)

Claim: Process for the production of Fonnkoks from coal of any kind, according to which the coal is gradually heated, partially oxidized and degassed in the fluidized bed, whereupon pretreated in this way Coal is mixed with a binding agent, briquetted and coked, characterized by the essentially known measures