WO2010090013A1 - コークス製造用粘結材の製造方法およびコークスの製造方法 - Google Patents
コークス製造用粘結材の製造方法およびコークスの製造方法 Download PDFInfo
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- WO2010090013A1 WO2010090013A1 PCT/JP2010/000655 JP2010000655W WO2010090013A1 WO 2010090013 A1 WO2010090013 A1 WO 2010090013A1 JP 2010000655 W JP2010000655 W JP 2010000655W WO 2010090013 A1 WO2010090013 A1 WO 2010090013A1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C3/00—Working-up pitch, asphalt, bitumen
- C10C3/08—Working-up pitch, asphalt, bitumen by selective extraction
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
- C10B55/02—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material with solid materials
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/14—Hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/005—Coking (in order to produce liquid products mainly)
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1077—Vacuum residues
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/80—Additives
Definitions
- the present invention relates to a method for producing a coking material for coke production and a method for producing coke, and particularly to a method for producing a coking material for coke production obtained from crude oil as a raw material and a method for producing coke.
- Blast furnace coke is a heat source that melts ores, a reducing agent that reduces iron ore to iron, and supports high temperatures to maintain gas permeability and melt permeability in the blast furnace.
- coke is required to have a sufficiently high strength that can withstand the pressure of the packed bed in the blast furnace and achieve a high porosity, and also has high wear resistance that can sufficiently reduce the generation of fine powder.
- it is preferable to contain a strong coking coal at a certain ratio or more in the raw coke for producing coke.
- crude oil is generally separated into gas, LPG, naphtha, kerosene, light gas oil, heavy gas oil, and atmospheric distillation residue by performing atmospheric distillation in the refining process.
- the naphtha separated from other components such as atmospheric distillation residue by the atmospheric distillation of the crude oil is usually separated into light naphtha and heavy naphtha after removing sulfur by hydrorefining equipment.
- the heavy naphtha is reformed by a catalytic reformer to be a reformate mainly composed of aromatic hydrocarbons. Thereafter, the reformate is separated by a rectification apparatus, and separated into a light reformate mainly composed of a hydrocarbon having 5 carbon atoms and a fraction mainly composed of an aromatic hydrocarbon having 6 or more carbon atoms. .
- the atmospheric distillation residue separated from other components by atmospheric distillation of the crude oil is usually further distilled under reduced pressure using a vacuum distillation apparatus.
- the vacuum distillation residue separated from other components by distillation under reduced pressure from the atmospheric distillation residue is a solvent extraction method called SDA (Solvent Deasphalting Process) process, a pyrolysis method such as a yurika process or a coker process, or Further purification by methods other than
- SDA solvent extraction method
- the solvent is used to selectively separate and remove the marten component consisting of a relatively low molecular weight oil and resin constituting the vacuum distillation residue, and to reduce the vacuum distillation residue.
- Asphaltene having an alkyl side chain and hydrogen contained in is concentrated to produce a viscous SDA pitch.
- a light oil with a high hydrogen content and a high carbonaceous oil pitch with a high softening point, such as yurika pitch are obtained by thermal decomposition of the vacuum distillation residue. Is broken down into When the pyrolysis method is performed on the vacuum distillation residue, the side chain of asphaltene contained in the vacuum distillation residue is dealkylated by the pyrolysis reaction, and a dehydrogenation reaction occurs. Therefore, the asphaltenes contained in petroleum pitch are those in which the asphaltenes contained in the vacuum distillation residual oil are modified, and are highly aromatic having undergone polycondensation.
- caking production caking materials made of petroleum pitch such as yurika pitch have been used by adding to coking coal when producing coke for iron making, and blending non-caking coal in coking coal for coke production. It is known that the rate can be increased.
- a caking material for coke production it is preferable that the asphaltene is less modified and an optically anisotropic structure is easily developed during the co-carbonization reaction with coal. The strength of coke can be improved, and the blending ratio of non-slightly caking coal can be increased (see Non-Patent Document 1).
- Examples of the caking material for coke production using crude oil as a raw material include those described in Patent Documents 1 to 4.
- Patent Document 1 butane, pentane or hexane is used alone or mixed as a solvent, and deasphalted asphalt having a softening point of 100 ° C. or higher obtained from petroleum heavy oil is added and blended as a caking additive.
- Patent Document 2 describes a method for producing artificial caking coal obtained by modifying deasphalted asphalt extracted with butane, pentane or hexane as a solvent by heat treatment.
- Patent Document 3 contains components that are soluble in hexane: more than 20% and 90% or less, components that are insoluble in toluene: 1% or less, the remainder being insoluble in hexane and soluble in toluene, and unavoidable
- Patent Document 4 discloses a first step in which a light oil is separated from petroleum heavy oil by solvent extraction or distillation to obtain a petroleum pitch, and a first step in which petroleum pitch is hydro-reformed and a reformed product is obtained.
- a method for producing a coking binder is described which has two steps and a third step of separating the modified product into light oil and heavy residue by solvent extraction or distillation extraction.
- the binder described in Patent Document 1 has a low softening point and contains a large amount of light paraffin. Therefore, the binder has a disadvantage that it is not preferable when used as a binder for coke production.
- the artificial caking coal described in Patent Document 2 is modified as a result of heat treatment of deasphalted asphalt, the asphaltene is denatured, and when used as caking material for coke production, When the development of optically anisotropic structure cannot be sufficiently promoted during the carbonization reaction, the effect of improving the strength of coke is insufficient, and the blending ratio of non-slightly caking coal cannot be increased sufficiently was there.
- none of the conventional techniques has a low volatile content, and it has been difficult to produce a good coke production caking material with high yield that can effectively improve the strength of coke. It was. That is, in order to obtain a coking material caking material that can effectively improve the strength of coke, pyrolysis as a method of refining vacuum distillation residue to prevent asphaltene denaturation due to thermal decomposition reaction. It is conceivable to use a solvent extraction method instead of the method. In the solvent extraction method, the heavier the solvent used, the smaller the volatile content of the resulting coke production binder, and the resulting coke production binder has a unit structure of coal. It is preferable because it has a similar aromaticity and can effectively improve the strength of coke.
- butane or pentane which is a hydrocarbon that is heavier (high molecular weight) than propane that is usually used in the SDA process, is used in the solvent extraction method.
- the method used as a solvent can be considered.
- the resulting coking material caking material contains a large amount of light paraffin with a low softening point. There will be no less. For this reason, in order to obtain a good binder for coke production with a small amount of volatile matter, it is necessary to use a hydrocarbon heavier than butane as a solvent. However, the heavier the solvent used, the higher the viscosity and softening point of the resulting coke production binder, making it difficult to remove the coke production binder from the solvent extractor. Productivity and yield of the caking material for production are reduced.
- the present invention has been made in view of the above problems, and can effectively improve the strength of coke, and can produce a good coke production caking material with low volatile content with high yield. It is an object to provide a manufacturing method. In addition, the present invention can add non-slightly caking coal with a high content to the coke production raw coal by using the coke production raw coal including the coke production binder of the present invention, and has high strength. It is an object of the present invention to provide a method for producing coke from which coke can be obtained.
- the method for producing a caking material for producing coke according to the present invention includes at least one of an atmospheric distillation residue obtained by atmospheric distillation of crude oil, and a vacuum distillation residue obtained by atmospheric distillation and vacuum distillation of crude oil.
- Light reformate obtained by catalytic reforming of naphtha fraction fractionated from crude oil by atmospheric distillation of residual oil containing one can be used as a caking additive for coke production.
- Including a step of extracting a solvent devoiding pitch is performed in the method for producing a caking additive for producing coke according to the present invention.
- the extraction of the solvent debris pitch is performed at an extraction temperature of 150 ° C.
- the softening point of the solvent debonding pitch is 140 to 200 ° C.
- the content of carbon remaining in the solvent debonding pitch is 30% by mass to 70%. It may be mass%.
- the caking material for producing coke according to the present invention is obtained by the above production method, and has a softening point of 140 to 200 ° C., a residual carbon content (residual carbon content) of 30 mass% to 70 mass%, hydrogen relative to carbon.
- the atomic ratio (H / C) is 1.2 or less.
- the method for producing coke according to the present invention includes a residual oil containing at least one of an atmospheric distillation residue obtained by atmospheric distillation of crude oil, and a vacuum distillation residue obtained by atmospheric distillation and vacuum distillation of crude oil.
- a solvent-removable pitch that can be used as a caking additive for coke production is obtained using light reformate obtained by catalytic reforming of the naphtha fraction fractionated from the crude oil by atmospheric distillation.
- the solvent deburring pitch may be contained in an amount of 0.5 to 10% by mass in the raw coke for producing coke.
- 10 to 50% by mass of non-slightly caking coal may be contained in the raw coal for producing coke.
- the asphaltene is not modified by the pyrolysis reaction.
- the binder for coke manufacture which can improve the intensity
- the solvent debris pitch is extracted from the residual oil using light reformate as a solvent, so that the volatile content is compared with the case where butane is used as the solvent. There are few, and it is easy to take out from a solvent extraction apparatus compared with the case where hexane is used as a solvent. Therefore, it is possible to produce a good caking production caking material with a high yield.
- non-slightly caking coal can be added at a high content in the coking coal for producing coke, and high strength coke can be obtained.
- the content in the raw material coal can be reduced.
- FIG. 1 is a flowchart for explaining an example of a method for producing a coking material for producing coke and a method for producing coke according to the present invention.
- FIG. 1 is a flowchart for explaining an example of a method for producing a coking material for producing coke and a method for producing coke according to the present invention.
- a solvent extraction device extracts a solvent debonding pitch that can be used as a caking manufacturing caking material from a residual oil using a light reformate as a solvent.
- an atmospheric distillation residue is obtained by atmospheric distillation of the crude oil by an atmospheric distillation apparatus used in the crude oil refining process. And this vacuum distillation residue is vacuum-distilled with a vacuum distillation apparatus, and a vacuum distillation residue is obtained.
- the vacuum distillation residue obtained in this way is used as a raw material for the solvent-developed pitch.
- a vacuum distillation residual oil obtained by atmospheric distillation and vacuum distillation of crude oil may be used as shown in FIG.
- An atmospheric distillation residue obtained by atmospheric distillation may be used, or a mixture of an atmospheric distillation residue and a vacuum distillation residue may be used.
- the light reformate used as a solvent is obtained by subjecting crude oil to atmospheric distillation to obtain a naphtha fraction, and reforming the naphtha fraction with a catalytic reformer. It is separated from the components of More specifically, the light reformate is obtained as follows. First, crude oil as a raw material is fractionated by an atmospheric distillation apparatus shown in FIG. 1 to obtain a naphtha fraction (mainly a fraction of 30 to 230 ° C.).
- the naphtha fraction is fractionated in advance into a light naphtha fraction (for example, corresponding to a boiling point of 30 to 90 ° C) and a heavy naphtha fraction (for example, corresponding to a boiling point of 80 to 180 ° C) by an atmospheric distillation apparatus, and then hydrorefined.
- a light naphtha fraction for example, corresponding to a boiling point of 30 to 90 ° C
- a heavy naphtha fraction for example, corresponding to a boiling point of 80 to 180 ° C
- heavy naphtha (mainly boiling point 80 to 180 ° C.) is reformed by a catalytic reformer to obtain a reformate mainly composed of aromatic hydrocarbons.
- the reformate thus obtained has a density of 0.78 to 0.81 g / cm 3 , a research octane number of 96 to 104, a motor octane number of 86 to 89, and an aromatic content of 50 to 70% by volume. , Which contains 30 to 50% by volume of the saturated content.
- the reformate is separated into a light reformate mainly composed of a hydrocarbon having 5 carbon atoms and a C6 + fraction by a rectifier.
- the C6 + fraction is mainly composed of aromatic hydrocarbons having 6 or more carbon atoms, and other components such as saturated hydrocarbons, olefinic hydrocarbons, and naphthenic hydrocarbons having 6 or more carbon atoms. It is a waste.
- Each component contained in the light reformate and the C6 + fraction can be determined by, for example, GC (gas chromatograph) analysis (JIS K2536 “Petroleum product-component test method”) or the like.
- the separation conditions for the light reformate and the C6 + fraction are not particularly limited as long as they can be separated so that benzene is not included in the light reformate.
- the C6 + fraction in the light reformate is 30% by volume or less. It adjusts suitably so that it may become.
- the light reformate thus obtained contains 5 to 15% by volume of butane, 60 to 80% by volume of pentane, and 5 to 30% by volume of hexane.
- butane, pentane, and hexane may be a mixture of normal paraffins and isoparaffins having 4, 5, and 6 carbon atoms, respectively.
- the residual oil and solvent are mixed by a mixing device such as a mixer of the solvent extraction device, and then the critical temperature above the critical pressure of the solvent. It supplies to the asphaltene separation tank of the solvent extraction apparatus maintained under the following constant conditions. Asphalt contained in the residual oil precipitates in the asphaltene separation tank. This precipitate is continuously extracted from the bottom of the asphaltene separation tank, and the slightly contained solvent is removed from the extracted precipitate by a stripper. As a result, a solvent escape pitch that can be used as a caking agent for producing coke is obtained.
- the oil extracted from the top of the asphaltene separation tank is used as deasphalted oil (DAO).
- DAO deasphalted oil
- the extraction temperature is set to 150 ° C to 200 ° C, and the flow rate ratio of the solvent to the residual oil (solvent / residual oil) is 5/1 to 8 / 1 is preferable.
- the extraction temperature of the residual oil is appropriately determined according to the properties of the residual oil, and is adjusted so that the softening point of the solvent removal pitch becomes constant.
- the extraction temperature is less than 150 ° C., the softening point of the solvent debonding pitch becomes 200 ° C. or more, and it becomes difficult to take out the binder for producing coke from the solvent extraction apparatus. Therefore, the productivity and yield of the caking material for coke production are reduced.
- the softening point of the solvent debonding pitch will be 140 ° C or less, which may make it difficult to mix with the raw coal or melt and fix in the summer coal storage. It is not preferable. Also, if the flow rate ratio of solvent to residual oil (solvent / residual oil) is less than 5/1, the amount of solvent is small, so the extraction efficiency in the asphaltene separation tank decreases, and the softening point of the solvent debris pitch is 140 It is not preferable in terms of handling because it may be less than or equal to ° C and may become difficult to mix with raw coal or melt and be fixed in a summer coal storage. When the ratio of solvent to residual oil (solvent / residual oil) exceeds 8/1, the solvent consumption is increased by circulating more solvent than necessary, resulting in uneconomical operation. Absent.
- the solvent devolatilized pitch thus obtained has a softening point of 140 to 200 ° C., and the carbon content (residual carbon content) remaining in the solvent devolatilized pitch is 30% by mass to 70% by mass. Yes, the atomic ratio of hydrogen to carbon (H / C) is 1.2 or less.
- the softening point referred to here is a value measured by JIS K2207 “Petroleum Asphalt-Softening Point Test Method (Ring and Ball Method)”.
- Residual carbon content (residual carbon content) is a value measured by JIS K2270 "Crude oil and petroleum products-Residual carbon content test method".
- the atomic weight ratio of hydrogen to carbon is a value measured according to ASTM D5291 “Standard Test Methods for Instrumental Determination of Carbon, Hydrogen, and Nitrogen in Petroleum Products and Lubricants”.
- ASTM D5291 Standard Test Methods for Instrumental Determination of Carbon, Hydrogen, and Nitrogen in Petroleum Products and Lubricants.
- the content of light paraffin with a low softening point is sufficiently small and the volatile content is also sufficiently small, so that excellent binding properties are obtained when used as a caking material for coke production. It is done.
- Coke is produced by carbonizing raw coal.
- the coking coal raw material coal preferably contains 0.5% by mass or more of the coke producing binder, more preferably 1% by mass or more.
- the amount of the coke producing caking additive contained in the coke producing raw coal is preferably 10% by mass or less, and more preferably 5% by mass or less.
- coking coal coking material contains 0.5 to 10% by mass of coke producing coking coal
- the proportion of non-slightly caking coal contained in coke producing raw coal is 10 to 50% by mass. Even if it does, it becomes possible to aim at the improvement of coke strength by addition of a caking additive.
- the non-slightly caking coal is contained in the raw coke for producing coke, and is contained in an amount of 15 mass% or more. More preferably. Moreover, it is preferable that the quantity of the non-slightly caking coal contained in raw coal for coke manufacture is 50 mass% or less, and it is preferable that it is 40 mass% or less.
- the non-slightly caking coal contained in the coking coal is within the above range, the coke strength can be improved by adding the caking additive, and the coking coal is maintained while maintaining the coke strength. The effect that content of the strong caking coal in inside can be reduced is acquired.
- the asphaltene is not modified by the pyrolysis reaction. Therefore, an excellent caking additive for producing coke that can effectively improve the strength of coke can be obtained. Further, according to the method for producing a caking material for coke production according to the present embodiment, since the solvent-removal pitch is extracted from the residual oil using light reformate as a solvent, an excellent caking material for producing coke with a low volatile content is obtained. Can be manufactured with good yield.
- non-slightly caking coal can be added at a high content in the coke production raw coal, and high strength coke can be obtained.
- the content in the raw coal for production can be reduced. That is, in the method for producing coke according to the present embodiment, since the coking material for coke production includes the caking material for coke production according to the present embodiment, the coke production raw material coal is used for coke production by dry distillation.
- the caking additive improves the adhesion of coal particles and promotes the development of an optically anisotropic structure during the co-carbonization reaction with coal. This improves the strength of the coke.
- Example shown below is an example for confirming the effect of this invention, and this invention is not limited to this example.
- the present invention can adopt various conditions as long as the object of the present invention is achieved without departing from the gist of the present invention.
- the atmospheric distillation residue is obtained by atmospheric distillation using the atmospheric distillation apparatus used in the crude oil refining process shown in FIG. 1, and the atmospheric distillation residue is subjected to vacuum distillation using the vacuum distillation apparatus. A residual oil was obtained. And from this atmospheric distillation residual oil, the solvent removal pitch was extracted using the solvent shown in Table 1. In this example, this solvent-developed pitch was used as a caking material for caking production (AB in Table 1). In addition, an atmospheric distillation residue is obtained by atmospheric distillation using an atmospheric distillation apparatus used in the crude oil refining process, and an atmospheric distillation residue is obtained by subjecting the atmospheric distillation residue to vacuum distillation using a vacuum distillation apparatus. Got.
- the atmospheric distillation residue was further pyrolyzed by the Yurika process to obtain Yurika pitch.
- this yurika pitch (commercial petroleum-based pitch) was used as a caking material for caking production (C in Table 1).
- the density, softening point, residual carbon, industrial analysis results, elemental analysis results, and composition analysis results of the caking materials A to C for coke production thus obtained are shown in Table 1 together with the test methods.
- the light reformate is 7% by volume of butane (a mixture of normal butane and isobutane), 66% by volume of pentane (a mixture of normal pentane and isopentane), and hexane (of normal hexane and isohexane). 27% by volume).
- the coke production binder A using light reformate as a solvent has a higher softening point than coke production binder B using butane as a solvent, and coke made of yurika pitch. It was lower than the caking material C for production, and was a preferable range as the caking material for producing coke.
- the ratio (H / C ratio) of residual carbon content and hydrogen and carbon was also a preferable range as the caking material for coke manufacture.
- the coke of the comparative example 1 was manufactured by dry-distilling the raw coal for coke manufacture containing 20 mass% of non-slightly caking coal, and 80 mass% of caking coal using a coke oven.
- 5% by mass of the coke producing caking material A or the coke producing caking material C shown in Table 1 is added to the coke producing raw coal using the coke of Comparative Example 1 at the time of production, and dry distillation is performed. Coke of Example 1 and Reference Example 1 was produced.
- CSR Coke Strenghafter-CO 2 Reaction
- the wear strength was measured by adding 200 g of coke with a particle size of 20 mm into a circular tube made of steel having a diameter of 130 mm and a length of 700 mm, sealing it, and rotating it at a rotation speed of 20 rpm for 600 revolutions, and remaining the weight on the 9.5 mm sieve. Rated by rate.
- the fluidity was evaluated by the following method. In other words, non-slightly caking coal was used as the base charcoal, and 5% by mass of caking materials for AC coke production was added to the base charcoal. The maximum fluidity (MF) was obtained. An apparent MF (log-ddpm (Dial Division Per Minute)) and an expansion rate (%) of the flow temperature range width were determined.
- the apparent binder MF (log-ddpm) is the apparent maximum fluidity of the binder for producing coke, and was determined by the following equation.
- Binder apparent MF ((Maximum fluidity of base charcoal containing binder-Maximum fluidity of base charcoal) x Base charcoal content) / Binder content ratio
- expansion rate of flow temperature range width (% ) Is the expansion ratio (%) of the flow temperature range width expanded from the flow temperature range width of the base coal (solidification temperature-softening start temperature) by the addition of the caking additive for coke production.
- the coking material binding material A obtained using light reformate as a solvent the coking material binding material B obtained using butane as a solvent, or coke manufacturing which is a yurika pitch.
- the apparent binder MF (log-ddpm) and the expansion rate (%) of the flow temperature range are large, and the effect of improving the fluidity and the flow temperature range is large. I understood.
- the reason why the flow temperature range is widened is the decrease in the softening start temperature, and the difference in the flow temperature range in the caking materials A to C is presumed to be due to the difference in the asphaltene content. .
- the present invention can produce high-strength coke even if the blending ratio of non-slightly caking coal is increased, and is highly industrially useful.
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Abstract
Description
本願は、2009年2月3日に出願された特願2009-23053について優先権を主張し、その内容をここに援用する。
原油を常圧蒸留することにより常圧蒸留残油等の他の成分から分離されたナフサは、通常、水素化精製装置で硫黄分を除去された後、軽質ナフサと重質ナフサとに分離される。重質ナフサは、接触改質装置によって改質されて芳香族系炭化水素を主体とするリフォーメートとされる。その後、リフォーメートが精留装置によって分離され、炭素数5の炭化水素を主成分とするライトリフォーメートと、炭素数6以上の芳香族系炭化水素を主成分とする留分とに分離される。
減圧蒸留残油のSDAプロセスでは、溶剤により、減圧蒸留残油を構成している比較的低分子量のオイルとレジンとからなるマルテン分が選択的に分離されて除去されるとともに、減圧蒸留残油に含まれていたアルキル側鎖や水素を有するアスファルテンが濃縮されて、粘稠なSDAピッチが生成される。
特許文献1には、ブタン、ペンタンもしくはヘキサンを単独または混合して溶剤として使用し、石油系重質油より得られた軟化点100℃以上の脱れきアスファルトを、粘結材として添加・配合する技術が記載されている。
特許文献2には、ブタン、ペンタンまたはヘキサンを溶剤として抽出した脱れきアスファルトを、熱処理によって改質してなる人造粘結炭の製造方法が記載されている。
また、特許文献4には、石油系重質油から溶剤抽出または蒸留処理により軽質油を分離して石油ピッチを得る第一工程と、石油ピッチを水素化改質処理して改質物を得る第二工程と、改質物を溶剤抽出または蒸留抽出により軽質油と重質残渣とに分離する第三工程とを有するコークス製造用粘結材の製造法が記載されている。
また、特許文献2に記載の人造粘結炭は、脱れきアスファルトを熱処理によって改質しているため、アスファルテンが変性しており、コークス製造用粘結材として用いた場合に、石炭との共炭素化反応時に光学的異方性組織構造の発達を十分に促すことできず、コークスの強度を向上させる効果が不足して、非微粘結炭の配合割合を十分に増加させることができない場合があった。
すなわち、コークスの強度を効果的に向上させることができるコークス製造用粘結材を得るためには、熱分解反応によるアスファルテンの変性を防止するために、減圧蒸留残油を精製する方法として熱分解法ではなく溶剤抽出法を用いることが考えられる。また、溶剤抽出法においては、用いる溶剤が重質であるほど、得られるコークス製造用粘結材の揮発分が少なくなるし、得られるコークス製造用粘結材の分子構造が石炭の単位構造に似た芳香族性の高いものとなり、コークスの強度を効果的に向上できるため好ましい。したがって、揮発分の少ない良好なコークス製造用粘結材を得るためには、SDAプロセスにおいて通常用いられるプロパンよりも重質な(分子量の大きい)炭化水素であるブタンやペンタンを、溶剤抽出法の溶剤として用いる方法が考えられる。
また、本発明は、本発明のコークス製造用粘結材を含むコークス製造用原料炭を用いることにより、コークス製造用原料炭中に高い含有量で非微粘結炭を添加でき、しかも高強度のコークスが得られるコークスの製造方法を提供することを課題とする。
本発明のコークス製造用粘結材の製造方法において、前記溶剤脱れきピッチの抽出を、抽出温度を150℃~200℃、前記残油に対する前記溶剤の流量比(溶剤/残油)を5/1~8/1として行ってもよい。
本発明のコークス製造用粘結材の製造方法においては、前記溶剤脱れきピッチの軟化点が140~200℃であり、前記溶剤脱れきピッチ中に残留する炭素の含有量が30質量%~70質量%であってもよい。
本発明のコークスの製造方法においては、前記コークス製造用原料炭中に、前記溶剤脱れきピッチが0.5~10質量%含まれていてもよい。
本発明のコークスの製造方法においては、前記コークス製造用原料炭中に、非微粘結炭が10~50質量%含まれていてもよい。
また、本発明のコークス製造用粘結材の製造方法によれば、残油から、ライトリフォーメートを溶剤として溶剤脱れきピッチを抽出するので、溶剤としてブタンを用いた場合と比較して揮発分が少なく、溶剤としてヘキサンを用いた場合と比較して溶剤抽出装置から取り出しやすい。したがって、良好なコークス製造用粘結材を歩留まりよく製造できる。
図1は、本発明のコークス製造用粘結材の製造方法およびコークスの製造方法の一例を説明するためのフローチャート図である。図1に示す本実施形態の製造方法では、溶剤抽出装置において、残油から、ライトリフォーメートを溶剤として、コークス製造用粘結材として使用可能な溶剤脱れきピッチを抽出する。
なお、溶剤脱れきピッチの原料として使用する残油としては、図1に示すように、原油を常圧蒸留および減圧蒸留することにより得られる減圧蒸留残油を使用してもよいが、原油を常圧蒸留することにより得られる常圧蒸留残油を使用してもよいし、常圧蒸留残油と減圧蒸留残油との混合物を使用してもよい。
まず、原料である原油を図1に示す常圧蒸留装置によって分留して、ナフサ留分(主に30~230℃の留分)を得る。ナフサ留分は、常圧蒸留装置によって軽質ナフサ留分(例えば沸点30~90℃相当)と重質ナフサ留分(例えば沸点80~180℃相当)とに予め分留して、その後水素化精製(水素化脱硫処理)しても良いし、水素化精製(水素化脱硫処理)装置でナフサ留分を処理した後、軽質ナフサと重質ナフサに分留しても良い。
続いて、接触改質装置によって重質ナフサ(主として沸点80~180℃)を改質して芳香族系炭化水素を主体とするリフォーメートとする。このようにして得られたリフォーメートは、密度が0.78~0.81g/cm3、リサーチ法オクタン価が96~104、モーターオクタン価が86~89であり、芳香族分を50~70容量%、飽和分を30~50容量%含むものである。
ライトリフォーメートとC6+留分との分離条件は、ライトリフォーメート中にベンゼンが含まれないように分離できれば特に限定されるものではないが、例えばライトリフォーメート中のC6+留分が30容量%以下となるように適宜調整される。
このようにして得られたライトリフォーメートは、ブタンを5~15容量%、ペンタンを60~80容量%、ヘキサンを5~30容量%含むものである。なお、ここでいうブタン、ペンタン、ヘキサンとは、各々炭素数4、5、6のノルマルパラフィンとイソパラフィンの混合物であっても良い。
残油の抽出温度は、残油の性状に応じて適宜決定されるものであって、溶剤脱れきピッチの軟化点が一定となるように調整される。抽出温度が150℃未満であると、溶剤脱れきピッチの軟化点が200℃以上となり、溶剤抽出装置内からコークス製造用粘結材を取り出すことが困難となる。そのため、コークス製造用粘結材の生産性および歩留まりが低下する。抽出温度が200℃を超えると、溶剤脱れきピッチの軟化点が140℃以下となり、原料石炭への配合が困難になったり、夏場の貯炭場で溶融固着したりする恐れがあり、ハンドリング面で好ましくない。
また、溶剤と残油との流量比(溶剤/残油)が5/1未満であると、溶剤が少ないため、アスファルテン分離槽での抽出効率が低下し、溶剤脱れきピッチの軟化点が140℃以下となり、原料石炭への配合が困難になったり、夏場の貯炭場で溶融固着したりする恐れがあり、ハンドリング面で好ましくない。溶剤と残油との比(溶剤/残油)が8/1を超えると、必要以上の溶剤を循環させることで、溶剤抽出装置のエネルギー消費量が増大し、非経済的な運転となり、好ましくない。
なお、ここでいう軟化点とは、JIS K2207「石油アスファルト‐軟化点試験方法(環球法)」により測定した値である。残留する炭素の含有量(残留炭素分)とは、JIS K2270「原油及び石油製品‐残留炭素分試験方法」により測定した値である。炭素に対する水素の原子量比(H/C)とは、ASTM D5291“Standard Test Methods for Instrumental Determination of Carbon,Hydrogen,and Nitrogen in Petroleum Products and Lubricants”に準拠して、測定される値である。
このような溶剤脱れきピッチにおいては、軟化点の低い軽質パラフィンの含有量が十分に少なく、揮発分も十分に少ないので、コークス製造用粘結材として用いた場合に、優れた結合性が得られる。
コークス製造用原料炭中には、コークス製造用粘結材が0.5質量%以上含まれていることが好ましく、1質量%以上で含まれていることがより好ましい。また、コークス製造用原料炭中に含まれるコークス製造用粘結材の量は10質量%以下であることが好ましく、5質量%以下であることがより好ましい。
コークス製造用原料炭中にコークス製造用粘結材が0.5~10質量%含まれている場合、コークス製造用原料炭中に含まれる非微粘結炭の割合を10~50質量%にしたとしても、粘結材の添加によりコークス強度の向上を図ることが可能となる。
コークス製造用原料炭中に含まれる非微粘結炭が上述の範囲であれば、粘結材の添加によりコークス強度の向上を図ることができ、またコークス強度を維持しつつコークス製造用原料炭中における強粘結炭の含有量を低減できるという効果が得られる。
すなわち、本実施形態のコークスの製造方法においては、コークス製造用原料炭に本実施形態のコークス製造用粘結材が含まれているので、コークス製造用原料炭を乾留することにより、コークス製造用粘結材が、石炭粒子の接着性を向上させるとともに、石炭との共炭素化反応時に光学的異方性組織構造の発達が促される。このことにより、コークスの強度が向上する。
また、原油の精製工程において用いられる常圧蒸留装置によって原油を常圧蒸留することにより常圧蒸留残油を得、この常圧蒸留残油を減圧蒸留装置によって減圧蒸留することにより減圧蒸留残油を得た。そしてこの常圧蒸留残油を、ユリカプロセスによってさらに熱分解することによりユリカピッチを得た。本実施例では、このユリカピッチ(市販石油系ピッチ)をコークス製造用粘結材(表1中のC)として使用した。
このようにして得られたコークス製造用粘結材A~Cの密度、軟化点、残留炭素、工業分析結果、元素分析結果、組成分析結果を、試験法とともに表1に示す。
表1に示すように、溶剤としてライトリフォーメートを用いたコークス製造用粘結材Aの軟化点は、溶剤としてブタンを用いたコークス製造用粘結材Bと比較して高く、ユリカピッチからなるコークス製造用粘結材Cと比較して低く、コークス製造用粘結材として好ましい範囲であった。
また、コークス製造用粘結材Aは、残留炭素分や水素と炭素との比(H/C比)もコークス製造用粘結材として好ましい範囲であった。
また、比較例1のコークスを製造時に使用したコークス製造用原料炭に、表1に示すコークス製造用粘結材Aまたはコークス製造用粘結材Cを5質量%添加し、乾留することにより実施例1および参考例1のコークスを製造した。
の結果を表2に示す。
なお、CSRは、以下に示す方法により測定した。すなわち、粒度20mmのコークス200gを1100℃の高温でCO2ガスと2時間反応させたのち、室温でI型ドラムにより回転強度を測定する方法により行った。
磨耗強度は、鋼鉄製の直径130mm、長さ700mmの円形の筒内に、粒径20mmのコークスを200g投入して密閉し、回転速度20rpmで600回転させた後の9.5mm篩上重量残率によって評価した。
また、コークス製造用粘結材Aを用いた実施例1のコークスでは、コークス製造用粘結材を用いない比較例1のコークスと比較して、磨耗強度が優れていることが確認できた。
流動性の評価は、以下に示す方法により行った。すなわち、非微粘結炭をベース炭とし、A~Cのコークス製造用粘結材をベース炭に対して5質量%添加し、ギーセラープラストメーター法(JIS M 8801)による流動性評価試験を実施し、最高流動度(MF:Maximum Fluidity)を得た。粘結材見掛けMF(log-ddpm (Dial Division Per Minute))と流動温度範囲幅の拡大率(%)とを求めた。
粘結材見掛MF=((粘結材を配合したベース炭最高流動度-ベース炭最高流動度)×ベース炭含有率)/粘結材含有率
また、流動温度範囲幅の拡大率(%)は、ベース炭の流動温度範囲幅(固化温度-軟化開始温度)からコークス製造用粘結材の添加により拡大した流動温度範囲幅の拡大率(%)である。
なお、流動温度範囲幅を広げている要因は、軟化開始温度の低下であり、コークス製造用粘結材A~Cにおける流動温度範囲幅の差は、アスファルテン含有率の違いによるものと推察される。
Claims (7)
- 原油を常圧蒸留して得られる常圧蒸留残油、および原油を常圧蒸留および減圧蒸留して得られる減圧蒸留残油の少なくともいずれかひとつを含む残油から、原油を常圧蒸留することにより前記原油から分留されるナフサ留分を接触改質して得られるライトリフォーメートを溶剤として、コークス製造用粘結材として使用可能な溶剤脱れきピッチを抽出する工程を含むコークス製造用粘結材の製造方法。
- 前記溶剤脱れきピッチの抽出を、抽出温度を150℃~200℃、前記残油に対する前記溶剤の流量比を5/1~8/1として行う請求項1に記載のコークス製造用粘結材の製造方法。
- 前記溶剤脱れきピッチの軟化点が140~200℃であり、前記溶剤脱れきピッチ中に残留する炭素の含有量が30質量%~70質量%である請求項1または請求項2に記載のコークス製造用粘結材の製造方法。
- 請求項1から3のいずれかに記載の製造方法により得られるコークス製造用粘結材であって、
軟化点が140~200℃、残留する炭素の含有量が30質量%~70質量%、炭素に対する水素の原子数比が1.2以下であるコークス製造用粘結材。 - 原油を常圧蒸留して得られる常圧蒸留残油、および原油を常圧蒸留および減圧蒸留して得られる減圧蒸留残油の少なくともいずれかひとつを含む残油から、原油を常圧蒸留することにより前記原油から分留されるナフサ留分を接触改質して得られるライトリフォーメートを溶剤として、コークス製造用粘結材として使用可能な溶剤脱れきピッチを抽出する工程と、
前記溶剤脱れきピッチを含むコークス製造用原料炭を乾留することによりコークスを得る工程とを備えるコークスの製造方法。 - 前記コークス製造用原料炭中に、前記溶剤脱れきピッチが0.5~10質量%含まれている請求項5に記載のコークスの製造方法。
- 前記コークス製造用原料炭中に、非微粘結炭が10~50質量%含まれている請求項5または請求項6に記載のコークスの製造方法。
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JP (1) | JP4576463B2 (ja) |
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- 2010-02-03 US US13/138,332 patent/US9493708B2/en active Active
- 2010-02-03 BR BRPI1008161-5A patent/BRPI1008161B1/pt active IP Right Grant
- 2010-02-03 KR KR1020117020144A patent/KR101610989B1/ko active IP Right Grant
- 2010-02-03 CN CN201080006350.9A patent/CN102300957B/zh active Active
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CN103278610A (zh) * | 2013-06-08 | 2013-09-04 | 武汉钢铁(集团)公司 | 最大基氏流动度≤2000ddpm焦煤煤质的评价方法 |
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CN103995964B (zh) * | 2014-05-09 | 2017-07-21 | 武汉钢铁(集团)公司 | 建立瘦煤煤质评价模型的方法 |
Also Published As
Publication number | Publication date |
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BRPI1008161B1 (pt) | 2018-03-06 |
CN102300957A (zh) | 2011-12-28 |
US20110284424A1 (en) | 2011-11-24 |
KR20110121694A (ko) | 2011-11-08 |
CN102300957B (zh) | 2014-04-02 |
BRPI1008161A2 (pt) | 2016-03-08 |
JP4576463B2 (ja) | 2010-11-10 |
JP2010180287A (ja) | 2010-08-19 |
US20150001131A1 (en) | 2015-01-01 |
US9493708B2 (en) | 2016-11-15 |
KR101610989B1 (ko) | 2016-04-08 |
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