TW201406945A - Process and device for the production of metallurgical coke from petrol coal obtained in petroleum refineries by carbonisation in non-recovery or heat-recovery coke ovens - Google Patents

Abstract

The invention relates to a process for the production of metallurgical coke from petrol coal obtained in petroleum refineries by carbonisation in non-recovery or heat-recovery coke ovens, said process being based on petrol coal which is obtained or produced in petroleum refineries and which from the start has a volatile content of 15 to 19 wt. % and and an ash content of up to 2 wt. %, and which is fed in compacted form to a coke oven of the non-recovery or heat-recovery type for cyclic carbonisation, said coke oven being equipped with at least one separately heated burner so that the primary heating space or the secondary heating space below the coke oven chamber or both are heated to a temperature between 1000 DEG C and 1550 DEG C, and the volatile content contained in the petrol coal completely degasses within a period of less than 120 h, a metallurgical coke with a CSR strength of at least 44 % and a CRI reactivity of less than 33% being obtained and being suitable for use as metallurgical coke. The invention also relates to a coke oven which is designed according to the non-recovery or heat-recovery type and equipped with a primary heating space provided with burners heating the primary heating space.

Description

Method and apparatus for preparing metallurgical coke by carbonizing gasoline coal obtained from a refinery in a non-recovery or heat recovery coke oven

The present invention relates to a method for preparing metallurgical coke by carbonizing gasoline coal obtained from a refinery in a non-recovered or heat recovery coke oven based on gasoline coal obtained or prepared in a refinery, and the gasoline coal From the beginning, having a volatile content of 15 wt.% to 19 wt.% and an ash content of up to 2 wt.%, and feeding it to the non-recovery or heat recovery coke oven in a compacted form for cyclic carbonization, the coke oven is equipped Having at least one independently heated burner thereby heating the primary heating space or the secondary heating space below the coke oven chamber or both to a temperature between 1000 ° C and 1550 ° C, and in less than 120 hours During the time period, the volatiles contained in the gasoline coal are completely degassed, thereby obtaining a metallurgical coke having a CSR strength of at least 44% and a CRI reactivity of less than 33%, and which is suitable for use as a metallurgical coke. The present invention also relates to a coke oven designed according to the non-recovery or heat recovery type and equipped with a main heating space having a burner for heating the main heating space.

When processing mineral oil and petroleum into petroleum products in a refinery, in addition to obtaining the desired products, so-called gasoline coke is obtained, which is processed by the distillation process, recombination step, hydrogenation process and purification operation of the refinery. The residue is formed by boiling at a high temperature. This gasoline coke is typically composed of more than 88 wt.% carbon and 8 wt.% to 12 wt.% volatile components (volatile Constituent, VOC) composition. This gasoline coke has only minimal economic benefit because it has some undesirable characteristics, such as low CSR strength and high CRI reactivity, for many applications, and for this reason it cannot be easily marketed.

Gasoline coke is commonly used in suitable applications such as metallurgical processes for making electrodes. It is not possible to use gasoline coke in a metallurgical plant, for example as a reducing agent in a blast furnace process to produce coarse iron, since the strength of the gasoline coke is insufficient for use in a blast furnace. Furthermore, it is known to mix several gasoline coke portions into a hard coal mixture, however, the mixed portion of the gasoline coke is limited to a value of less than 10 wt.% due to the low level of blast furnace coke produced therefrom.

Another problem with gasoline coke is that it is derived from impurities in petroleum processing, and when the coke has been discharged, impurities still accumulate in the coke. Common impurities in gasoline char are, for example, vanadium, nickel, sulfur, antimony, iron or titanium. Therefore, the vanadium content in the gasoline coke portion may be at most 0.17 wt.%, the nickel content is at most 0.04 wt.%, and the sulfur content is at most 5 wt.%. These impurities make gasoline coke unusable for heating purposes as this will affect the environment. Another characteristic of gasoline coke is that the flame temperature is lower than that of blast furnace coke or coal. This is undesirable for use as a fuel and its treatment, and therefore it cannot be used in many subsequent processes. Therefore, there is an opportunity to seek a possible economic application of providing gasoline coke.

In addition, the root cause of preventing metallurgical coke from being manufactured in such a manner that the carbonization process is suitable for gasoline coke characteristics, in addition to impurities and lack of product strength, is also a volatile component of the fluctuating portion. The volatile component of the fluctuating portion makes it difficult to predict the use in the coke oven because the heating characteristics are difficult to predict due to the volatile components. Typically, the major portion of gasoline coke produced in a refinery contains less than 19 wt.% of very low volatile components, so gasoline coke is not suitable for maintaining self-sustaining combustion when used in non-recovery or heat recovery coke ovens. The process and thus the carbonization process cannot be maintained. In fact, if only gasoline char is used as the raw material in the coke oven, the carbonization process will end after several carbonization cycles because the heat generated by the combustion of the volatile components during the carbonization and stored in the refractory of the furnace is no longer Sufficient to maintain the furnace temperature at a desired high value in excess of 1000 °C during subsequent batches.

Another difficulty in utilizing coal carbonization is that in carbonization, gasoline coke is characterized by extremely high expansion pressures, and this is due to the low boiling point of the volatile components contained therein. During carbonization, these features result in a significant increase in the volume of the coke cake, which is in fact "expanded." Therefore, it is impossible to carbonize gasoline coal in a conventional coke oven because the wall of the coke oven chamber will be damaged by the increase in the volume of the gasoline coal cake during carbonization. The increase in the volume of gasoline briquettes caused by the characteristics of the gasoline briquettes mentioned also makes it difficult to introduce coal char products made from the gasoline coke portion of the hard coal mixture into conventional coke oven chambers.

One possibility for processing and further use of gasoline coke is given in WO0010914A1. The teachings provide a method in which a gasoline coke derived from a refinery and a gasoline coke precursor material derived from mineral oil undergoes a thermal recombination process at a suitable pressure and a sufficiently high temperature for a length of time sufficient At that time, gasoline char is obtained, which contains a low and precisely adjustable volatile content of 13 wt.% to 50 wt.%. The method also discloses the possibility of deionizing gasoline char to remove metal impurities contained therein. Finally, the teachings also disclose the possibility of reducing the sulfur impurities in the gasoline char to a lower and environmentally acceptable portion, for example by adding a desulfurizing agent to the fluidized bed. The method provides the possibility of providing a gasoline char portion having a relatively accurately calculated volatile component and impurity content. The gasoline coke portion having a volatile portion of 15 wt.% to 25 wt.% is similar in characteristics to the conventional dry steam coal or fat coal, also referred to as "petrol coal".

The availability of gasoline coal with precisely quantifiable portions of volatile components and impurities provides a new possibility to produce metallurgical coke using the obtained gasoline coal. In the petroleum processing process, a particularly high portion of gasoline coal having a volatile content of 15 wt.% to 19 wt.% is produced. As of now, the problem of low energy content, low cost efficiency, dangerous expansion pressure during carbonization, large amounts of impurities and high combustion losses associated with this product cannot be solved by conventional carbonization processes, so this product has not been carried out on an industrial scale. machining. However, laboratory testing of metallurgical coke made from this particular fraction of gasoline coke has determined that the metallurgical coke has a good rating. Examples related to such tests The teachings of Stukov et al., "Increasing the Strength of Met-allurgical Petroleum Coke to the Coking Batch", Coke and Chemistry. 2009, Vol. 52, No. 8, pp. 349-352. Since the technical feasibility of manufacturing metallurgical coke from gasoline coal has not been safely treated so far, it is necessary to obtain a practicable method for manufacturing metallurgical coke by carbonization of gasoline coal.

Accordingly, it is an object to provide a method of providing gasoline coal having a volatile component of 15 wt.% to 19 wt.% and an increased portion of impurities, which is carbonized on an industrial scale using the gasoline coal and produces coal char. Coal char has increased strength and low reactivity and is suitable for use as a metallurgical coke.

The present invention achieves this object by providing a gasoline having a known volatile component content of 15 wt.% to 19 wt.% and a known ash fraction of up to 2 wt.%, and then under normal conditions. The carbonized coal in a compacted form is carbonized into metallurgical coke in a heating chamber of a non-recovery or heat recovery type coke oven at a temperature between 1000 ° C and 1550 ° C, and the furnace is equipped with At least one burner for heating a primary heating space containing a residual gas space above the gasoline coal cake during operation, or for heating a secondary heating space below the coke oven chamber, or both.

The volatile content and ash content of the gasoline coke are determined by analysis prior to carbonization, regardless of whether the analysis is carried out prior to the coke oven plant or the gasoline coal supplier. For the specific example of the method embodying the present invention, it is only important to provide a gasoline coal having a known volatile component content, and the observed volatile component content is in the range of at least 15 wt.% and up to 19 wt.%. .

In order to compensate for the reduced energy content of gasoline coal with the mentioned properties due to the lower fraction of volatile components, the main heating space or secondary heating space must be heated with external fuel gas, as only this low-energy gasoline coal portion is desired Processed into metallurgical coke in a non-recovery or heat recovery coking reactor. In addition, due to the low energy content of the raw materials, the temperature is maintained for a long time. At temperatures above 1000 ° C and therefore insufficient to compensate for the high exhaust gas and radiation losses that are necessarily associated with the process, an extremely long and uneconomical carbonization period will result.

However, the use of a non-recycled or heat recovery type coke oven allows the carbonization of a feed mixture consisting essentially of gasoline coal and having the properties mentioned, since such coke ovens provide a residual gas space above the gasoline briquettes during operation, This gas space absorbs the gradually increasing expansion pressure of the gasoline coal. Within the framework of the present invention, it has been determined that the coal char grade thus obtained is characterized by a CSR strength of more than 44% and a CRI reactivity of less than 33%, and therefore, such coal char grades can be used, for example, in metallurgical or blast furnace processes. Metallurgical coke in the middle. If the coal char is used in a blast furnace process, the coal char values mentioned will have a beneficial effect on the blast furnace process.

The invention particularly claims a method for producing metallurgical coke from gasoline coal obtained in the petroleum processing industry, wherein

. Analysis of the volatile matter content and ash content of the gasoline coke from the petrochemical process, whereby the batch can be sorted according to the batch having the known volatile component content and the ash content, and

. A gasoline coal batch having a volatile content of 15 wt.% to 19 wt.% and an ash content of less than 2 wt.% (referred to as an anhydrous ashless gasoline coal batch) is sorted and fed into a coal storage bin or a coal storage vessel.

. This portion of the gasoline coal from the coal storage bin or coal storage vessel is first fed into the compactor by means of a feeder and then fed to a coke oven having a non-recovered or heat recovery type for cyclic carbonization, and the method Characterized by

. The coke oven is equipped with at least one independently heated burner for heating a primary heating space above the gasoline coal cake or for heating a secondary heating space below the coke oven chamber, the burner being used in hot fuel gas With the help of heating the gasoline coal in the coke oven chamber to a temperature between 1000 ° C and 1550 ° C in less than 120 hours, thereby obtaining a CSR strength value of at least 44% and a CRI reactivity value is not To 33% metallurgical coke.

Those skilled in the art of carbonization are known to be equipped with primary and secondary heating spaces. Non-recovery or heat recovery coke ovens. Such a construction is described in detail in, for example, the article by Walter Buss et al., "Thyssen Still Otto/PACTI Non-recovery coke making system", Iron and Steel Engineer, Association of Iron and Steel Engineers, Pittsburgh, USA, Vol. 76, No. 1. Period, January 1999, pp. 33-38. An example of a coke oven group consisting of a coke oven suitable for carbonizing coal having a high expansion pressure is provided in WO2011107198A1. When heated, the gasoline briquettes reach an estimated temperature of 900 ° C to 1100 ° C.

The gasoline coal is heated by heating over the compacted gasoline coal cake, thereby producing a coal char of the desired grade in which the volatile components are derived from the batch in the form of a crude coke. In this case, heat is first produced in a substoichiometric manner by first burning a portion of the degassed component in the primary heating space by at least occasionally adding air. Subsequently, the partially combusted exhaust gas mixture is discharged by means of the side air passages of the coke oven chamber, and is completely combusted by further combustion in the secondary heating space. Since the gasoline coal contains a volatile portion, the gasoline coal is also heated from below, so that the gasoline briquettes are heated from all sides except the side door region and a uniform carbonization quality is obtained.

The grade of coal char obtained can be determined as described to obtain a CSR strength value of at least 44% and a CRI reactivity value of less than 33%. The precondition is to use a gasoline coal batch having a volatile content of 15 wt.% to 19 wt.% and an ash fraction of less than 2 wt.%, which is referred to as an anhydrous ashless gasoline coal batch.

It is also possible to use gasoline coal whose volatile component content is more accurately determined. In a specific embodiment of the invention, the volatile content of the gasoline coal is from 16 wt.% to 18 wt.%. Therefore, the method can be controlled more easily.

In general, for a specific embodiment of the invention, the gasoline briquettes can be heated from all sides to thereby achieve the desired temperature. In an advantageous embodiment of the invention, the coke oven is heated in such a way that the burner flame is horizontally buried in the gas space above the gasoline coal batch, the so-called main heating space. In an advantageous embodiment, at least one of the gas spaces above the gasoline coal is extended via the opening by means of a burner containing hot gas or combustion gases and via an opening. The piping is located in the wall above the door of the coke oven chamber whereby the gas space is heated by hot gases. The horizontal arrangement of the combustion tubes above the batch ensures that the inflowing gas above the gasoline briquettes flows into the main heating space and, therefore, reduces the direct contact between the coal surface and the combustion air and thereby reduces unwanted coal or coal char Burn out. At the same time, the vertical distance from the buried combustion tube to the upper edge of the batch is set to exceed 100 mm, so that the upper gasoline coal seam does not burn.

Within the framework of the invention, it is also possible, for example, to heat the gasoline coal by means of other burners arranged in the secondary heating space below the gasoline coal. In another embodiment, it is claimed that at least one burner is disposed separately or simultaneously on the side front opening of the secondary heating space, and therefore, the temperature of the heating space is also increased to increase the heating of the batch from below. Finally, it is also possible to use the top opening of the coke oven chamber for heating. A wall-heated coke oven as disclosed, for example, in US Pat. No. 4,045,299 A is feasible, even if it has not been tested in the present invention.

This heating can be set, for example, with the aid of ventilation and pressure control of the coke oven chamber, whereby a pressure of 0.01 to 20 mbar is set in the coke oven chamber. This can be achieved by correspondingly controlling the burner and the venting flap. In a preferred embodiment of the invention, the heating is set with the aid of ventilation and pressure control, whereby a pressure of 0.1 to 10 mbar is set in the coke oven chamber.

The coke oven chamber can be heated, for example, by natural gas or fuel gas. However, the coke oven chamber can also be heated by using liquefied gas, coke oven gas, blast furnace gas or converter gas as fuel gas. For specific embodiments embodying the process of the invention, it is also possible to use any portion of the mixture of at least two gases from the group of natural gas, liquefied gas, coke oven gas, blast furnace gas or converter gas for heating. The choice of fuel gas depends on various factors such as availability.

In order to achieve the desired CSR strength and CRI reactivity of the coal char product, and in order to ensure the desired heat capacity with the help of the heating ability of the degassing component, the adjustment of the volatile component content of the supplied gasoline coal is extremely important. . In a specific embodiment of the present invention, the gasoline coal mixture is mixed with the hard coal as an additive prior to pulverization, thereby setting the volatile content. Set between 19 wt.% and 25 wt.%, referred to as a dry feed mixture. In another embodiment, the gasoline coal mixture is mixed with the bitumen as an additive prior to comminution, thereby setting the volatiles content between 19 wt.% and 25 wt.%, referred to as the dry feed mixture. In another embodiment, the gasoline coal mixture is mixed with the oil grade as an additive prior to comminution, thereby setting the volatile content between 19 wt.% and 25 wt.%, referred to as dry feed. mixture. The coal char product thus obtained has a CSR strength of more than 44% and a CRI reactivity of less than 33%.

In addition, the gasoline coal used has less than 2 wt.% of the ash portion due to the process steps for obtaining the coal. Typically, this ash portion is just sufficient to protect the gasoline coal from being burned out excessively during carbonization. However, to ensure that the process is cost effective, additional measures are often required to prevent the gasoline coke from experiencing unwanted burnouts. For this reason, if gasoline coal is mixed with an additive having an inhibitory effect on the combustion of gasoline coal, a slightly higher volatile component content may be selected.

If the gasoline coal is mixed with additives that have an effect on the burning behavior of the gasoline coal, even a higher ash portion can be selected. The purpose of this ash portion is to avoid undesired burning of gasoline coal. In a specific embodiment of the invention, the gasoline coal mixture is mixed with the ash as an additive, whereby the ash portion is set between 2 wt.% and 12 wt.%, preferably 2 wt.% to 6 wt.%, referred to as total The mixture was dried, and the mixture was pulverized and sieved to obtain a portion having a particle size distribution d of 0.5 < d < 3 mm, and the sieved mixture was fed to a coal storage tank or a coal storage container for further carbonization. In order to distribute the ash in the product so that the CSR strength and CRI reactivity achieved are not changed in an unfavorable manner, pulverization and sieving are necessary.

In another embodiment, the gasoline coal mixture is mixed with the ash-containing coal as an additive, thereby setting the ash portion between 2 wt.% and 12 wt.%, preferably 2 wt.% to 6 wt.%, The mixture was total dried, and the mixture was pulverized and sieved to obtain a portion having a particle size distribution d of 0.5 < d < 3 mm, and the sieved mixture was fed to a coal storage tank or a coal storage container for further carbonization. The gasoline coal mixture may be completely or partially comminuted in the pulverizing apparatus before or after the additive is mixed, thereby obtaining a residue portion having an average particle size of less than 3 mm. Can also This comminution operation is carried out on a total mixture of partial fractions. Some of the scores are preferably 70 to 95 weight fractions, and some fractions are preferably 80 to 90 weight fractions.

Within the framework of the present invention, it is also possible to vary the water content of the produced gasoline coal by adding water. Adding water improves the stability of the gasoline briquettes. In a specific embodiment of the present invention, the total water content of the feed mixture is set at 7 wt.% to 11.5 wt.% by adding liquid water, and the mixture is fed to a coal storage tank or a coal storage container for further carbonization. . Water can be added directly and can also be added by spraying or immersion.

Within the framework of the invention and prior to use, the feed mixture can be compacted by means of either type of compactor, whereby the density of the feed mixture is from 0.8 t/m ³ to 1.225 t/m ³ . In general, the compacting operation can be carried out by extrusion, mashing, hammering or vibrating steps, which can also be combined. Prior to use, the feed mixture is preferably compacted by means of a mashing device whereby the density of the feed mixture is from 1.0 t/m ³ to 1.150 t/m ³ .

In order to affect the carbonization operation, a separation layer inert to combustion may be applied to the surface of the furnace cake before heating. This separation layer is composed, for example, of coal char. In another embodiment, the separation layer that is inert to combustion is comprised of coal. Finally, the separation layer which is inert to combustion may also consist of ash or sand. Finally, the separation layer that is inert to combustion may be composed of carbonaceous breeze (eg, coal dust or coal coke having a particle size of less than 25 mm).

In a specific embodiment of the invention, the separation layer has a thickness of from 0.2 cm to 25 cm. The separation layer can be applied as needed. Thus, the separation layer can be applied to the compacted coal mass, for example by means of a coal compactor, which is equipped with a feed port which is arranged on or between the stamps. To this end, there is a need for a coal compaction apparatus that includes at least one tamper and is equipped with a feed device above the batch. Coal compactors equipped with crushing, hammering, vibrating and squeezing devices for compaction are presently advanced and are described, for example, in WO2010102714A2.

In another embodiment, the additive is stored in a particular shaft in the coal storage bin, and the additive is fed from the shaft to a designated opening of the coal compactor during the feeding operation of the compacted coal mass. The additive can be fed to a designated opening of the coal compactor by means of a screw conveyor. Thus, the additive can also be fed to a designated opening of the coal compactor by means of a sliding system, a chain conveyor system, a gravity device or a chute. The separation layer can also be poured on the surface of the batch later and not in the compactor.

In another embodiment of the invention, in four continuous mixing chambers, the feed mixture is mixed with an additive, and the mixing of the comminuted and comminuted stock is carried out in the mixing chambers. The comminution and mixing can also be carried out in several stages. The feed mixture can also be preheated. Thus, the temperature of the feed mixture can be set between 120 ° C and 250 ° C, for example, by preheating in a heatable vessel prior to feeding to the coke oven.

Metallurgical coke obtained from gasoline coal can be used for other applications where necessary. It is especially useful as a blast furnace coke. However, it can also be used in non-ferrous metallurgical industries to make metals or to prepare electrodes.

It is also claimed to carry out the means by which the method of the invention is carried out. In particular, a coke oven for preparing coal char from gasoline coal obtained in the petroleum processing industry is proposed. Is a non-recovery or heat recovery type coking ovens, having a width of 2 to 6m of the coke oven chamber and 10 to 20m length of the coke oven chamber, whereby the height is 2m, the coke oven chamber volume of 40 to 240m ^3, And The coke oven has a masonry arch structure, and in the filling condition, together with the coke oven chamber located below, a gas space above the coal cake can be formed to serve as a main heating space, and The coke oven is equipped with a side flue and a secondary heating space below the coal, and The coke oven chamber is equipped with a coal storage bin or a coal storage container and a feeding machine, and the feeding device can feed the coking furnace chamber from the coal storage bin or the coal storage container, and the coke oven is characterized by: The coke oven chamber is heated with the aid of an external burner that heats the main heating space, and the burners extend into the gas gathering mains in the burner via an adjustable branch line along the front of the coke oven chamber. Fuel gas and oxygen-containing gas are supplied.

If necessary, an external burner can be placed on the coke oven chamber to promote primary heating Heating of the space. One or several external burners may be arranged in each coke oven chamber. However, in a preferred embodiment, the (these) burners are located in the wall of the coke oven chamber door above the coke oven chamber door on at least one side of the coke oven chamber, and are used to surround the coke oven chamber door The opening in the wall heats the main heating space. The orifice section of the combustion tube is introduced into the gas space via this opening.

To this end, the (these) burners are located in the wall of the coke oven chamber door above the coke oven chamber door on at least one side of the coke oven chamber and are heated primarily by openings located in the wall surrounding the coke oven chamber door The heating space, in an advantageous embodiment, sets the vertical distance from the combustion nozzle to the upper edge of the gasoline coal batch to exceed 100 mm. The arrangement of the burner on the top of the coke oven chamber saves space.

In a specific embodiment of the invention, the combustion nozzle or the combustion nozzles are made of heat resistant steel. In another embodiment, the (s) combustion nozzle is made of a refractory ceramic material. If multiple burners are installed, this can be seen on one or several burners.

In a preferred embodiment of the present invention, the coke oven embodying the present invention is combined with a plurality of other coke ovens to form a coke oven group, and the gas collection trunk line is erected along the front portion of the coke oven chamber of the coke oven group. Those skilled in the art of coking are known to assemble non-recovery or heat recovery coke ovens into a coke oven group.

The secondary heating space may also be heated by means of one or several external burners that are supplied with fuel gas via a gas gathering main line extending into the burner along the adjustable branch line at the front of the coke oven chamber. Oxygen gas. In one embodiment of the invention, the (these) burners are designed as ventilated burners. For this particular example, the gas collection mains can be located, for example, on top of the coke oven chamber. The gas collection mains can also be installed under the platform of the coke oven maintenance machine or along the pillars. Finally, the gas collection trunks can be arranged as needed to ensure the supply of burners.

The branch line can be controlled, for example, by means of a stopcock, a gate valve, a nozzle, a baffle or an orifice plate. In a specific embodiment of the invention, the coke oven group is equipped with a pressure control station in which the pressure of the fuel gas is reduced to a desired value, thereby passing the fuel gas from the pressure control station through the gas gathering The mains are fed to the burner and supplied directly at a suitable pressure for the burner.

A compactor is also claimed which is used to compact coal and is adapted to apply a separation layer to the compacted coal mass when preparing the compacted mass. Suitable compactors that can be used in this device assembly are described in WO201D102714A2. This machine consists of six tampers used as sides to prepare a compacted block by means of a squeezing device. In one embodiment of the invention, the tamper is operated hydraulically. A suitable compactor can also be formed by a vibrating device. For the compactor assembly embodying the invention, the upper ram or upper plate of the vibrating device of the compactor of WO2010102714A2 is provided with a tipping device by means of which the additive can be fed onto the surface of the compacting block, Thereby another additive layer fed by the tipping device appears on the surface of the compacted feed mixture during compaction.

A coke oven group is also claimed which consists of a coke oven embodying the invention and is equipped with the compactor.

The method embodying the invention is primarily carried out in a coke oven group consisting of a coke oven chamber embodying the invention along with additional prior art devices. It includes, for example, 1 to 10 levels of storage bins in which different gasoline coal feed mixtures are stored. It also includes, for example, 1 to 4 comminuting devices, 1 to 4 sieving devices or 1 to 4 mixing bins in which gasoline coal, additives or the entire feed mixture is stored, sieved and mixed. The coke oven group can also be equipped with a compactor.

The invention has the advantage of providing a possible economic application for gasoline coal, which is obtained in a refinery and a mineral oil processing industry and has a gasoline coke portion having a volatile content of 15 wt.% to 19 wt.%. By making coal char with a CSR strength of more than 44% and a CRI reactivity of less than 33%, the char can be used in a blast furnace process or in a metallurgical process to produce metal in contrast to carbonized gasoline coke.

In the following, analytical methods for gasoline coke are described, which are used to provide gasoline coal for use as feed gasoline coal embodying the method of the present invention.

1. Volatile content. The volatile content of gasoline char is determined, for example, according to DIM 51720. The portion of the residue that was still under vacuum within 7 minutes after heating of the coal was measured. A method for the rapid determination of volatiles in coal is provided in US 6074205A.

2. Ash content. The ash content is determined, for example, according to DIN 51719. The residue in the measuring furnace was still 815 ° C after burning coal. A method for the rapid determination of ash content in coal is provided in DE 31 2006 4 A1.

3. Coal coke strength. Coal coke strength is determined by a so-called CSR test. CSR is the abbreviation of "Coke Strength after Reaction". The weight percentage of the residue was measured and the residue was heated from 200 bar of carbon dioxide (CO ₂ ) to 1100 ° C for 2 hours and then to 600 minutes per minute (min ^-1 ) in a drum. Obtained after 30 minutes of treatment. Today, this test method is generally accepted, standardized and described, for example, in EP07387B0B2.

4. Coal coke reactivity. Coal coke reactivity is determined by a so-called CRI test. CRI is the abbreviation of "Coke Reactivity Index" and describes the chemical reactivity of coal char. The weight percentage of the residue was measured, which was obtained by heating 200 g of the char sample to 1100 ° C under 1 bar of carbon dioxide (CO ₂ ) for 2 hours. The value obtained is called CRI reactivity. The smaller the value obtained, the lower the reactivity. This method can be performed easily and quickly and the characteristic value CRI is well correlated with the behavior of coal char in the blast furnace process. Today, this test method is generally accepted, standardized according to ISO 18894 and described, for example, in EP 1 142 978 A1.

Claims (51)

A method for preparing metallurgical coke from gasoline coal obtained in the petroleum processing industry, wherein the gasoline content from the petrochemical process is analyzed for volatile matter content and ash content, thereby being capable of being batched according to known volatile component content and ash content The material is sorted and a gasoline coal batch having a volatile content of 15 wt.% to 19 wt.% and an ash content of less than 2 wt.% is selected, which is called an anhydrous ashless gasoline coal batch, and is fed to The coal storage bin or coal storage container, and the gasoline coal portion from the coal storage bin or coal storage container are first fed into the compactor by a feeder and then fed to a non-recycled or heat recovery type. Circulating carbonization in a coke oven characterized in that the coke oven is equipped with at least one independently heated burner for heating a main heating space above the gasoline coal cake or for heating a secondary heating space below the coke oven chamber Or both, the burner is used to heat the gasoline coal in the coke oven chamber to a temperature between 1000 ° C and 1550 ° C in less than 120 hours with the help of hot fuel gas. Thereby, a metallurgical coke having a CSR intensity value of at least 44% and a CRI reactivity value of less than 33% is obtained. The method of claim 1, wherein the gasoline coal has a volatile content of 16 wt.% to 18 wt.% before carbonization. The method of claim 1 or 2, wherein the coke oven is heated by burying the burner flame in the gas space above the gasoline coal batch. The method of any one of claims 1 to 3, wherein the coke oven is equipped with at least one externally heated burner for heating the secondary below the gasoline briquettes Heating space and for heating the gasoline briquettes. The method of claim 4, wherein the coke oven is heated by burying the burner flame in a gas space below the gasoline coal batch. The method of any one of claims 1 to 5, wherein the heating is set with the aid of ventilation and pressure control, thereby setting a pressure of 0.01 to 20 mbar in the coke oven chamber . The method of any one of claims 1 to 5, characterized in that the heating is set with the aid of ventilation and pressure control, thereby setting a pressure of 0.01 to 10 mbar in the coke oven chamber . The method of any one of claims 1 to 7, characterized in that the natural gas is used as a fuel gas for heating. The method of any one of claims 1 to 7, characterized in that the liquefied gas is used as the fuel gas for heating. The method according to any one of the items 1 to 7, characterized in that the coke oven gas is used as the fuel gas for heating. The method according to any one of the items 1 to 7, characterized in that the blast furnace gas is used as the fuel gas for heating. The method of any one of claims 1 to 7, characterized in that the converter gas is used as the fuel gas for heating. The method of any one of claims 8 to 12, characterized in that any part of a mixture of at least two gases from the group consisting of natural gas, liquefied gas, coke oven gas, blast furnace gas or converter gas is used. Heat up. The method of any one of claims 1 to 13, wherein the gasoline coal mixture is mixed with the hard coal as an additive before the pulverization, whereby the volatile matter content is set at 19 wt.% and 25 wt. Between .% is called a dry feed mixture. The method of any one of claims 1 to 13, wherein the gasoline coal mixture is mixed with the asphalt as an additive before the pulverization, whereby the volatile content is set at 19 wt.% and 25 wt. Between %, called the dry feed mixture. The method of any one of claims 1 to 13, wherein the gasoline coal mixture is mixed with an oil grade as an additive before the pulverization, whereby the volatile content is set at 19 wt. Between .% and 25 wt.% is referred to as a dry feed mixture. The method of any one of claims 1 to 16, wherein the gasoline coal mixture is mixed with ash as an additive, whereby the ash portion is set between 2 wt.% and 12 wt.%, It is referred to as a total dry mixture, and this mixture is pulverized and sieved before carbonization to obtain a portion having a particle size distribution d of 0.5 < d < 3 mm, and the sieved mixture is fed to the coal storage tank or coal storage container to further Carbonization. The method of any one of claims 1 to 16, wherein the gasoline coal mixture is mixed with the ash-containing coal as an additive, whereby the ash portion is set at 2 wt.% and 12 wt.%. Between, referred to as the total dry mixture, and this mixture is pulverized and sieved before carbonization, thereby obtaining a portion having a particle size distribution d of 0.5 < d < 3 mm, and the sieved mixture is fed to the coal storage bin or coal storage. The container is further carbonized. The method of claim 18, wherein the gasoline coal mixture is mixed with the ash-containing coal as an additive, whereby the ash portion is set between 2 wt.% and 6 wt.%, which is called a total dry mixture. And the mixture is pulverized and sieved before carbonization to obtain a portion having a particle size distribution d of 0.5 < d < 3 mm, and the sieved mixture is fed to the coal storage tank or the coal storage container for further carbonization. The method of any one of claims 14 to 19, characterized in that even before or after the additives are mixed, even the gasoline coal mixture is completely or partially pulverized in the pulverizing apparatus, thereby obtaining an average particle size smaller than 3mm residue part. The method of any one of claims 1 to 20, wherein the total water content of the feed mixture is set at 7 wt.% to 11.5 wt.% by adding liquid water, and the mixture Feed to the coal storage bin or coal storage vessel for further carbonization. The method of any one of clauses 1 to 21, wherein the feed mixture is compacted by means of a compactor prior to use, whereby the density of the feed mixture is 0.8 t /m ³ to 1.225 t/m ³ . The method of any one of clauses 1 to 21, wherein the feed mixture is compacted by means of a mashing device before use, whereby the density of the feed mixture is 1.0 t /m ³ to 1.150 t/m ³ . The method of any one of claims 1 to 23, wherein a separation layer inert to combustion is applied to the surface of the cake before heating. The method of claim 24, wherein the separation layer which is inert to combustion is composed of coal char. The method of claim 24, wherein the separation layer which is inert to combustion is composed of coal. The method of claim 24, wherein the separation layer which is inert to combustion is composed of carbonaceous coal dust having a particle size of less than 25 mm. The method of claim 24, wherein the separation layer which is inert to combustion is composed of ash or sand. The method of any one of claims 24 to 28, wherein the separation layer has a thickness of from 0.2 cm to 25 cm. The method of any one of claims 24 to 29, wherein the separation layer is applied to the compacted coal mass by means of a coal compactor equipped with a designation The feed port is arranged on the upper hammer or the upper plate. The method of any one of claims 24 to 30, wherein the additive is stored in a particular shaft in the coal storage bin, the additive being fed from the shaft to the shaft during the feeding operation The designated opening of the coal compactor. The method of claim 31, wherein the additive is fed to the designated opening of the coal compactor by means of a screw conveyor. The method of claim 31, wherein the additive is fed to the designated opening of the coal compactor by means of a sliding system. The method of claim 31, wherein the additive is fed to the designated opening of the coal compactor by means of a chain conveyor system. The method of any one of claims 24 to 34, wherein the feed mixture is mixed with the additives in up to four consecutive mixing chambers, and the mixing of the pulverized and pulverized storage materials is Wait for the mixing chamber. The method of any one of claims 1 to 35, wherein the temperature of the feed mixture is preheated to 120 ° C to 250 ° C in a heatable vessel prior to feeding the coke oven. A coke oven for preparing coal char from gasoline coal obtained in the petroleum processing industry, the coke oven belongs to a non-recovery or heat recovery coke oven type, which has a coke oven chamber width of 2 to 6 m and a coke oven chamber length of 10 to 20 m. degree, whereby the height is 2m, the coke oven chamber volume of 40 to 240m ^3, and the coke oven having a masonry arch of masonry, in filled condition, which may be positioned beneath the coke oven chamber of Forming a gas space above the coal cake for use as a main heating space, and the coke oven is equipped with a side flue and a secondary heating space located below, and the coke oven chamber is equipped with a coal storage bin or a coal storage container And a feeding machine, wherein the feeding machine can feed the coke oven chamber from the coal storage bin or the coal storage container, wherein the coke oven chamber is heated by the help of an external burner, and the external burner heats the main heating space And the burners are supplied with the fuel gas and the oxygen-containing gas via a gas gathering main line extending into the burners along the front portion of the coke oven chamber and the adjustable branch line. The coke oven of claim 37, wherein the burner is located on at least one side of the coke oven chamber and surrounds the wall of the coke oven chamber door above the coke oven chamber door, and The primary heating space is heated using an opening in the wall surrounding the door of the coke oven chamber, and the vertical distance from the burner nozzle to the upper edge of the batch is set to exceed 100 mm. A coke oven according to claim 37 or 38, wherein the combustion nozzle is made of heat resistant steel. A coke oven according to claim 37 or 38, characterized in that the burner nozzle is made of a refractory ceramic material. The coke oven according to any one of claims 37 to 40, characterized in that the coke oven is combined with another plurality of coke ovens to form a coke oven group, and the gas gathering main line is along the coke oven The front of the coke oven chamber of the group is erected. A coke oven according to any one of claims 37 to 41, wherein the secondary heating space is also heated by means of an external burner via the front of the coke oven chamber The gas collection mains are supplied with fuel gas and oxygen-containing gas, and the gas collection mains extend into the burner via an adjustable branch line. A coke oven according to any one of claims 37 to 42, wherein the burner is designed as a ventilating burner. A coke oven according to any one of claims 37 to 43 wherein the gas collection mains are located on top of the coke oven chamber. A coke oven according to any one of claims 37 to 44, wherein the gas gathering main line is located below the platform of the coke oven maintenance machine. A coke oven according to any one of claims 37 to 45, characterized in that the (s) branch line is controlled by means of a stopcock, a gate valve, a baffle, a nozzle or an orifice plate. A coke oven according to any one of claims 37 to 45, characterized in that the coke oven group is equipped with a pressure control station in which the pressure of the fuel gas is lowered to a desired value. Thereby the fuel gas is fed from the pressure control station to the burners via the gas collection mains. A compactor for compacting coal, which consists of up to eight hammers, which are used to prepare compacted blocks by means of a compactor, characterized in that the compactor is provided with a dumping device By means of the tipping device, an additive can be supplied onto the surface of the compacting block, whereby during the compaction, another additive layer supplied by the tipping device grows on the surface of the compacted feed mixture . A compactor for compacting coal, as in claim 48, wherein the compactor for preparing the compacted block is equipped with a hydraulic squeezing device. A compactor for compacting coal according to claim 48, wherein the compactor for preparing the compacted block is formed by a vibrating device. The coke oven group according to any one of claims 37 to 50, wherein the coke oven group is equipped with a compactor according to any one of claims 48 to 50.