CA2157052A1 - Method of producing coke for the iron and steel industry - Google Patents
Method of producing coke for the iron and steel industryInfo
- Publication number
- CA2157052A1 CA2157052A1 CA002157052A CA2157052A CA2157052A1 CA 2157052 A1 CA2157052 A1 CA 2157052A1 CA 002157052 A CA002157052 A CA 002157052A CA 2157052 A CA2157052 A CA 2157052A CA 2157052 A1 CA2157052 A1 CA 2157052A1
- Authority
- CA
- Canada
- Prior art keywords
- coal
- coke
- binder
- hydrogenation
- vacuum
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 239000000571 coke Substances 0.000 title claims abstract description 27
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title claims abstract description 15
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 8
- 229910000831 Steel Inorganic materials 0.000 title abstract description 6
- 239000010959 steel Substances 0.000 title abstract description 6
- 239000003245 coal Substances 0.000 claims abstract description 25
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 20
- 239000011230 binding agent Substances 0.000 claims abstract description 19
- 238000004939 coking Methods 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 10
- 239000000654 additive Substances 0.000 claims abstract description 9
- 230000000996 additive effect Effects 0.000 claims abstract description 9
- 239000000295 fuel oil Substances 0.000 claims abstract description 4
- 238000005292 vacuum distillation Methods 0.000 claims abstract description 4
- 239000003575 carbonaceous material Substances 0.000 claims description 3
- 239000003208 petroleum Substances 0.000 claims description 3
- 238000009628 steelmaking Methods 0.000 claims 1
- 239000000203 mixture Substances 0.000 abstract description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 230000009257 reactivity Effects 0.000 abstract description 3
- 239000010779 crude oil Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 12
- 239000003921 oil Substances 0.000 description 8
- 229910052717 sulfur Inorganic materials 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 239000011593 sulfur Substances 0.000 description 7
- 238000002474 experimental method Methods 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000011301 petroleum pitch Substances 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000008602 contraction Effects 0.000 description 2
- 230000010339 dilation Effects 0.000 description 2
- -1 hydrogen Hydrogen Chemical class 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000008961 swelling Effects 0.000 description 2
- 239000011269 tar Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- UTPYTEWRMXITIN-YDWXAUTNSA-N 1-methyl-3-[(e)-[(3e)-3-(methylcarbamothioylhydrazinylidene)butan-2-ylidene]amino]thiourea Chemical compound CNC(=S)N\N=C(/C)\C(\C)=N\NC(=S)NC UTPYTEWRMXITIN-YDWXAUTNSA-N 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- 241000282320 Panthera leo Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000011335 coal coke Substances 0.000 description 1
- 239000002864 coal component Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 231100000206 health hazard Toxicity 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000012803 optimization experiment Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000003921 particle size analysis Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
- C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
Proposed is a method of producing coke for use in the manufacture of iron and steel, in particular foundry coke, by mixing charge coal and about 0.5 to 10 %, relative to the coal in the water-free and ash-free state, of a binder, and then coking the mixture. The aim is to produce coke with a relatively low reactivity, the highest possible unit density, the highest possible carbon content and the largest possible lump size. Used as the binder is a vacuum-hydrogenation residue produced in the vacuum distillation stage of the hydrogenation of short residues or heavy oils derived from crude oil, with the addition of an additive consisting of porous carbon bodies made, in particular, of material derived from coal.
Description
FILE, ~N 17~ THIS ~t~r~D~LJ 21 ~ 7 0 52 - ~T TRANSLATION
TRANSLATION Fl~OM GERMAN
Cokemaking Process for the Iron and Steel Industry The invention concerns a cokemaking process for the iron and steel industry, especially foundry coke.
Coal charges that are already suitable by nature without admixtures for producing a coke with the desired prope~ lies, like a specified lumpiness and specified abrasion behavior, are hardly available anymore in the required amounts.
In order to obtain the desired properties it is known in cokemaking especially production of foundry coke, that about 5% petroleum pitch (referred to the moisture- and ash-free coal charge) can be added to coal charges, which can already be a mixture of several coal components and coke breeze.
This binder is particularly unavoidable when foundry coke with a high percenlage of carbon is to be produced, since coke breeze is then coemployed as an important coal charge component.
Petroleum pitch is comparatively costly.
A production process for metallurgical coke is known from US-A-4,234,387 in which a coking coal blend with unfavorable coking properties is mixed with a binder, which is formed, for example, as a vacuum distillation residue from hydrogenation of heavy oils or bitumens; however, the vacuum distillation residue from hydrogenation of bitumens from tar sarlds is preferred.
21~70.~2 This binder is used in amounts of as much as 20%, preferably between 5 and 15% (re~erred to the coking coal blend). The initial blends so produced for the coking process exhibit relatively moderate dilation and contraction values. The greater the contraction, the greater the sintering effect of the finely divided coking coal particles at the beginning of gas expulsion of the coking coal, i.e., before its softening. Subsequent dilation as a result of swelling on further degassing of the coking coal is largely responsible for the structure of the coke skeleton. Cokes produced according to this known process therefore already have a comparatively low stability factor, as well as a comparatively low hardness factor - this means limited drum resistance, as well as relatively high abrasion.
With this as a point of departure the instructions of the patent claim solve the problem of producing a coke for the iron and steel industry with relatively limited reactivity, the ~ atesl possible lump density, the highest possible percentage of carbon and the coarsest possible lumpmess.
Because of the invention the base of useable binders is expanded and preferably a particularly cost-effective binder with the least possible health hazards is employed.
Experiments have shown that the binder according to the invention leads to coke properties equivalent to those during the use of so-called petroleum pitch, in which the binder according to the invention is much more cost-effective and contains very few carcinogenic components. In principle the process according to the invention is also employable in the production of blast furnace coke.
The additive in conjunction with the other charge materials of hydrogenation decisively matters, the additive preferably being added in an amount of 1 to 3 wt% referred to the total charge materials of hydrogenation. This additive consists of porous carbonaceous materials that consist, in particular, of material of coal origin and whose internal surface, if possible, is a few hundred, typically 300 m2/g.
21~70~2 This additive surprisingly has not only a reaction-stabilizing and quality-enhancing effect on the hydrogenation products, but also acts as a component of the vacuum hydrogenation residue as a framework-former for the coke skeleton in the coking process according to the invention.
Porous carbonaceous materials can be produced in a variety of ways and are generally known; their effect on the quality of coke, especially for the iron and steel industries, in conjunction with the process according to the invention, on the other hand, was in no way foreseeable.
Hydrogenation of petroleum and petroleum products, like heavy oils and vacuum residues, is known in itself and is described in the standard work concerning hydrogenation technology "Catalytic pressure hydrogenation of coals, tars and mineral oils" by Dr. Walter Kronig, Springer-Verlag, 1950. The hydrogenation conditions vary according to the charge material being hydrogenated. Tn each case it occurs with addition of hydrogen at elevated pressure and elevated temperature, in which typical reaction conditions are 100 to 300 bar system pressure at temperatures between 200 and 500OC. This high-pressure hydrogenationpreferably occurs in a so-called liquid-phase reactor. The product stream leaving the liquid-phase reactor consists of oils, solids and gases and is then separated into two phases, for example, in a hot sepa~ ~tor, namely an overhead product and a bottom product. The bottom product is separated in a subsequent vacuum column from distillable oils (vacuumhydrogenation residue).
The use of hydrogenation residue formed during hydrogenation according to the so-called VCC process (yEBA Combi-Cracking process) is particularly preferred according to the invention. The latest state of the VCC process was published on the occasion of the DGMK
main meeting of 1990 in Munster/Westphalia under the title "New aspects of the VCC
process" by Dr. Klaus Niemann. There is therefore no need to describe it further here.
21~70~S2 Practical Example An industrial VCC unit with 95% conversion processes the charge materials listed in Table I
and produces the products listed in Table 2. The charge materials are further specified in Table 3 and the products in Table 4. The solidified vacuum hydrogenation residue from the vacuum column to be used according to the invention had the chemical-physical properties and particle sizes listed in Table S and was then mixed in an industrial experiment at a coke plant as binder to a coal charge consisting of a mixture of 32.4% of a low-volatile coal with poor coking properties (noncoking coal), ~8.6% of a medium-volatile coal with good coking properties (prime coking coal) and 14.0% coke breeze, as well as S wt% vacuum hydrogenation residue, to produce foundry coke. The coking coal blend and the coke properties obtained after 33 hours of coking time are shown in Table 6. The obtained results with the vacuum hydrogenation residue used as binder according to the invention (right column of Table 6) were compared with the normal operational results of the coke plant (petroleum pitch as binder) according to the prior art (Table 6, left column).
Coking occurred in several ovens of an industrial coke oven battery (Otto design, chamber width 450 mm, chamber height 5.10 m, chamber length 13.1 m, volume 27.64 m3). This large experiment was preceded by many small experiments with the binder according to the invention and other mixing ratios on the order of 3 to 7% binder referred to the moisture-and ash-free coal charge. These pilot experiments were run as optimization experiments in comparison with the use of the usual binder.
The coke yields could be increased by the invention, as is appalellt from Table 6.
The binder according to the invention contains surprisingly few polycyclic aromatic hydrocarbons.
21570S~
-Table 1.
Charge materialskglh Vacuum residue166.666 Additive 1.667 Fresh hydrogen7.042 Tur~oine co,~ '12.750 Sum t88.125 Table 2.
Products kg/h MP gas 8.384 LP gas 13.045 01~ gas 18 Naphtha 24.081 Gas oil 86. j63 Vacuum gas oil31.525 Vacuum hydrogen residue 9.203 Dilute acid solution 15.306 Sum 188.125 2~57~52 Table 3. Specification of the charge materials.
Vacuum residue: Arabian Light TBP Ult. . ~.,CtiOI1 point C 565+
Density (15-C) kg/dm3 1.022 Carbon wt% 84.38 Hydrogen wt% 10.30 Sulfur wt% 4.34 Nitrogen wt% 0.38 Oxygen wt% 0.6 Ash wt% about 0.02 Solids not stated Nickel ppm by weight 25 Vanadium ppm by weight 114 Iron not stated Asphaltenes wt% 10 Conradson carbon wt% 20/3 Viscosity 50-C cSt 150,500 100-C cSt 1589 Additive Porous calbol-àce~,us ,..1. ,~ e from a coal material with an internal surface of about 300 m21g (is virtually u~,Ldng~,d by hyd,~gel~a~;oll to the extent detectable) Fresh hydrogen Hydrogen (Hz) min99.6 mol%
Nitrogen (Nz) max 0.2 mol%
Methane (CH~) max 0.1 mol%
thane (CzH6) max 0.1 mol%
21~70~2 Table 4. Specification of the product.
MP/LP gas: irlternal use Naphtha TBP boiling range C5+ -180 C
Sulfur <20 ppm l~itrogen <20 ppm Gasoline/Gas oil gap (ASTM D86 95/5%) min. 15 C
Gas oil lBP boiling range t80-343 C
Sulfur <100 ppm Water content <50 ppm Cetane number >38 Gas oil/Vacuum gas oil overlap (ATSM D86) 95/5% max. 30 C
Vacuum gas oil TBP boiling range 343 ~C+
Sulfur <600 ppm Nitrogen ~600 ppm Aniline point Metals .~ I ppm Solidified hydrogenation residue (contains the employed additive) TBP boiling range 524 C+
Analysis C 86.0 wt%
H 6.0 wt%
O 0.5 wt%
N 1.0 wt%
S 2.5 (2-4) v~t%
Inorganic cu.l",un.,l.t~ 4.0 (2-4) wt%
Solids (toluene-insoluble) 20-40 wt%
21570~2 -Table 5.
Chemical-Physical ~ ,.t;es Densiq (at 15-C)1300-1500 kg/m~
Bulk densiq 500-700 kg/m' Pour point 150 C
Flash point <200 C
Ignition t~ .dlulc; <400 C
Softening point120-160 C
Net calorific value 36 MJ/kg Gross calorific value 37 MJ/kg Volatile cvlll~ollc.lb 40-70 %
Particle size analysis 6.3 mm about 6 wt%
6.3-3.15mm about40 wt%
TRANSLATION Fl~OM GERMAN
Cokemaking Process for the Iron and Steel Industry The invention concerns a cokemaking process for the iron and steel industry, especially foundry coke.
Coal charges that are already suitable by nature without admixtures for producing a coke with the desired prope~ lies, like a specified lumpiness and specified abrasion behavior, are hardly available anymore in the required amounts.
In order to obtain the desired properties it is known in cokemaking especially production of foundry coke, that about 5% petroleum pitch (referred to the moisture- and ash-free coal charge) can be added to coal charges, which can already be a mixture of several coal components and coke breeze.
This binder is particularly unavoidable when foundry coke with a high percenlage of carbon is to be produced, since coke breeze is then coemployed as an important coal charge component.
Petroleum pitch is comparatively costly.
A production process for metallurgical coke is known from US-A-4,234,387 in which a coking coal blend with unfavorable coking properties is mixed with a binder, which is formed, for example, as a vacuum distillation residue from hydrogenation of heavy oils or bitumens; however, the vacuum distillation residue from hydrogenation of bitumens from tar sarlds is preferred.
21~70.~2 This binder is used in amounts of as much as 20%, preferably between 5 and 15% (re~erred to the coking coal blend). The initial blends so produced for the coking process exhibit relatively moderate dilation and contraction values. The greater the contraction, the greater the sintering effect of the finely divided coking coal particles at the beginning of gas expulsion of the coking coal, i.e., before its softening. Subsequent dilation as a result of swelling on further degassing of the coking coal is largely responsible for the structure of the coke skeleton. Cokes produced according to this known process therefore already have a comparatively low stability factor, as well as a comparatively low hardness factor - this means limited drum resistance, as well as relatively high abrasion.
With this as a point of departure the instructions of the patent claim solve the problem of producing a coke for the iron and steel industry with relatively limited reactivity, the ~ atesl possible lump density, the highest possible percentage of carbon and the coarsest possible lumpmess.
Because of the invention the base of useable binders is expanded and preferably a particularly cost-effective binder with the least possible health hazards is employed.
Experiments have shown that the binder according to the invention leads to coke properties equivalent to those during the use of so-called petroleum pitch, in which the binder according to the invention is much more cost-effective and contains very few carcinogenic components. In principle the process according to the invention is also employable in the production of blast furnace coke.
The additive in conjunction with the other charge materials of hydrogenation decisively matters, the additive preferably being added in an amount of 1 to 3 wt% referred to the total charge materials of hydrogenation. This additive consists of porous carbonaceous materials that consist, in particular, of material of coal origin and whose internal surface, if possible, is a few hundred, typically 300 m2/g.
21~70~2 This additive surprisingly has not only a reaction-stabilizing and quality-enhancing effect on the hydrogenation products, but also acts as a component of the vacuum hydrogenation residue as a framework-former for the coke skeleton in the coking process according to the invention.
Porous carbonaceous materials can be produced in a variety of ways and are generally known; their effect on the quality of coke, especially for the iron and steel industries, in conjunction with the process according to the invention, on the other hand, was in no way foreseeable.
Hydrogenation of petroleum and petroleum products, like heavy oils and vacuum residues, is known in itself and is described in the standard work concerning hydrogenation technology "Catalytic pressure hydrogenation of coals, tars and mineral oils" by Dr. Walter Kronig, Springer-Verlag, 1950. The hydrogenation conditions vary according to the charge material being hydrogenated. Tn each case it occurs with addition of hydrogen at elevated pressure and elevated temperature, in which typical reaction conditions are 100 to 300 bar system pressure at temperatures between 200 and 500OC. This high-pressure hydrogenationpreferably occurs in a so-called liquid-phase reactor. The product stream leaving the liquid-phase reactor consists of oils, solids and gases and is then separated into two phases, for example, in a hot sepa~ ~tor, namely an overhead product and a bottom product. The bottom product is separated in a subsequent vacuum column from distillable oils (vacuumhydrogenation residue).
The use of hydrogenation residue formed during hydrogenation according to the so-called VCC process (yEBA Combi-Cracking process) is particularly preferred according to the invention. The latest state of the VCC process was published on the occasion of the DGMK
main meeting of 1990 in Munster/Westphalia under the title "New aspects of the VCC
process" by Dr. Klaus Niemann. There is therefore no need to describe it further here.
21~70~S2 Practical Example An industrial VCC unit with 95% conversion processes the charge materials listed in Table I
and produces the products listed in Table 2. The charge materials are further specified in Table 3 and the products in Table 4. The solidified vacuum hydrogenation residue from the vacuum column to be used according to the invention had the chemical-physical properties and particle sizes listed in Table S and was then mixed in an industrial experiment at a coke plant as binder to a coal charge consisting of a mixture of 32.4% of a low-volatile coal with poor coking properties (noncoking coal), ~8.6% of a medium-volatile coal with good coking properties (prime coking coal) and 14.0% coke breeze, as well as S wt% vacuum hydrogenation residue, to produce foundry coke. The coking coal blend and the coke properties obtained after 33 hours of coking time are shown in Table 6. The obtained results with the vacuum hydrogenation residue used as binder according to the invention (right column of Table 6) were compared with the normal operational results of the coke plant (petroleum pitch as binder) according to the prior art (Table 6, left column).
Coking occurred in several ovens of an industrial coke oven battery (Otto design, chamber width 450 mm, chamber height 5.10 m, chamber length 13.1 m, volume 27.64 m3). This large experiment was preceded by many small experiments with the binder according to the invention and other mixing ratios on the order of 3 to 7% binder referred to the moisture-and ash-free coal charge. These pilot experiments were run as optimization experiments in comparison with the use of the usual binder.
The coke yields could be increased by the invention, as is appalellt from Table 6.
The binder according to the invention contains surprisingly few polycyclic aromatic hydrocarbons.
21570S~
-Table 1.
Charge materialskglh Vacuum residue166.666 Additive 1.667 Fresh hydrogen7.042 Tur~oine co,~ '12.750 Sum t88.125 Table 2.
Products kg/h MP gas 8.384 LP gas 13.045 01~ gas 18 Naphtha 24.081 Gas oil 86. j63 Vacuum gas oil31.525 Vacuum hydrogen residue 9.203 Dilute acid solution 15.306 Sum 188.125 2~57~52 Table 3. Specification of the charge materials.
Vacuum residue: Arabian Light TBP Ult. . ~.,CtiOI1 point C 565+
Density (15-C) kg/dm3 1.022 Carbon wt% 84.38 Hydrogen wt% 10.30 Sulfur wt% 4.34 Nitrogen wt% 0.38 Oxygen wt% 0.6 Ash wt% about 0.02 Solids not stated Nickel ppm by weight 25 Vanadium ppm by weight 114 Iron not stated Asphaltenes wt% 10 Conradson carbon wt% 20/3 Viscosity 50-C cSt 150,500 100-C cSt 1589 Additive Porous calbol-àce~,us ,..1. ,~ e from a coal material with an internal surface of about 300 m21g (is virtually u~,Ldng~,d by hyd,~gel~a~;oll to the extent detectable) Fresh hydrogen Hydrogen (Hz) min99.6 mol%
Nitrogen (Nz) max 0.2 mol%
Methane (CH~) max 0.1 mol%
thane (CzH6) max 0.1 mol%
21~70~2 Table 4. Specification of the product.
MP/LP gas: irlternal use Naphtha TBP boiling range C5+ -180 C
Sulfur <20 ppm l~itrogen <20 ppm Gasoline/Gas oil gap (ASTM D86 95/5%) min. 15 C
Gas oil lBP boiling range t80-343 C
Sulfur <100 ppm Water content <50 ppm Cetane number >38 Gas oil/Vacuum gas oil overlap (ATSM D86) 95/5% max. 30 C
Vacuum gas oil TBP boiling range 343 ~C+
Sulfur <600 ppm Nitrogen ~600 ppm Aniline point Metals .~ I ppm Solidified hydrogenation residue (contains the employed additive) TBP boiling range 524 C+
Analysis C 86.0 wt%
H 6.0 wt%
O 0.5 wt%
N 1.0 wt%
S 2.5 (2-4) v~t%
Inorganic cu.l",un.,l.t~ 4.0 (2-4) wt%
Solids (toluene-insoluble) 20-40 wt%
21570~2 -Table 5.
Chemical-Physical ~ ,.t;es Densiq (at 15-C)1300-1500 kg/m~
Bulk densiq 500-700 kg/m' Pour point 150 C
Flash point <200 C
Ignition t~ .dlulc; <400 C
Softening point120-160 C
Net calorific value 36 MJ/kg Gross calorific value 37 MJ/kg Volatile cvlll~ollc.lb 40-70 %
Particle size analysis 6.3 mm about 6 wt%
6.3-3.15mm about40 wt%
3.15-2.00 mm about 20 wt%
2.00-1.00 mm about 17 wt%
1.00-0.5 mm about 5 wt%
0.5 mm about 10 wt%
Table 6.
Normal operation withTest operation with 5% petroleum pitch5% h.ydl~,ge.l~.lion residue Cokin~ coal blend:
Water, wt% -8.0 -8.0 Ash. wt% -6.0 -6.0 Sulfur wt% 0.7S 0.86 Volatiie CO~pOII.,,.t~ (mf), wt%-19.0 -18.3 Residue: Carbon Degree of swelling -6.0 -5.0 Sulfur in binder, wt% -0 -2.7 Coking time, h 33 33 Coke l,.op~,.li~,~.
Drum .e;,(~ .cc M80 (DIN), % 83.0 81.0 Abrasion M10 (DIN) 5.6 6.0 Lump density, g/cm3 n.d. -1.05 Specific weight, g/cml n.d. -1.92 Porosity, vol% n.d. -46.0 Reactivity, km n.d. 0.18 Sulfur (mf), wt% 0.69 0.78 Ash (mf), wt% -6.8 7.0 Coke yields, % 73 -76
2.00-1.00 mm about 17 wt%
1.00-0.5 mm about 5 wt%
0.5 mm about 10 wt%
Table 6.
Normal operation withTest operation with 5% petroleum pitch5% h.ydl~,ge.l~.lion residue Cokin~ coal blend:
Water, wt% -8.0 -8.0 Ash. wt% -6.0 -6.0 Sulfur wt% 0.7S 0.86 Volatiie CO~pOII.,,.t~ (mf), wt%-19.0 -18.3 Residue: Carbon Degree of swelling -6.0 -5.0 Sulfur in binder, wt% -0 -2.7 Coking time, h 33 33 Coke l,.op~,.li~,~.
Drum .e;,(~ .cc M80 (DIN), % 83.0 81.0 Abrasion M10 (DIN) 5.6 6.0 Lump density, g/cm3 n.d. -1.05 Specific weight, g/cml n.d. -1.92 Porosity, vol% n.d. -46.0 Reactivity, km n.d. 0.18 Sulfur (mf), wt% 0.69 0.78 Ash (mf), wt% -6.8 7.0 Coke yields, % 73 -76
Claims
Cokemaking process for iron and steelmaking especially foundry coke, by mixing coal charges and about 0.5 to 10%, referred to the moisture- and ash-free coal charge, of a binder, as well as subsequent coking, in which a vacuum hydrogenation residue is used as binder, which is formed during vacuum distillation of hydrogenation, when vacuum residues or heavy oils of petroleum origin are hydrogenated with addition of an additive consisting of a porous carbonaceous material, especially a material of coal origin.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP4306057.9 | 1993-02-26 | ||
| DE4306057A DE4306057A1 (en) | 1993-02-26 | 1993-02-26 | Method of making foundry coke |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2157052A1 true CA2157052A1 (en) | 1994-09-01 |
Family
ID=6481457
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002157052A Abandoned CA2157052A1 (en) | 1993-02-26 | 1994-02-25 | Method of producing coke for the iron and steel industry |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP0686180A1 (en) |
| JP (1) | JPH08509509A (en) |
| AU (1) | AU6206794A (en) |
| CA (1) | CA2157052A1 (en) |
| DE (2) | DE4306057A1 (en) |
| WO (1) | WO1994019425A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2808412C1 (en) * | 2022-12-20 | 2023-11-28 | Акционерное общество "ТАИФ" | Method for processing heavy petroleum raw materials |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE745161C (en) * | 1939-01-01 | 1944-02-28 | Ig Farbenindustrie Ag | Process for the production of tar and solid coke |
| DE1696503A1 (en) * | 1961-10-06 | 1970-05-14 | Great Lakes Carbon Corp | Process for the production of metallurgical coke |
| CA1114765A (en) * | 1978-04-28 | 1981-12-22 | Keith Belinko | Production of metallurgical coke from poor coking coals using residue from processed tar sand bitumen |
| US4999328A (en) * | 1988-06-28 | 1991-03-12 | Petro-Canada Inc. | Hydrocracking of heavy oils in presence of petroleum coke derived from heavy oil coking operations |
-
1993
- 1993-02-26 DE DE4306057A patent/DE4306057A1/en not_active Withdrawn
-
1994
- 1994-02-25 DE DE4490891T patent/DE4490891D2/en not_active Expired - Fee Related
- 1994-02-25 WO PCT/EP1994/000555 patent/WO1994019425A1/en not_active Application Discontinuation
- 1994-02-25 CA CA002157052A patent/CA2157052A1/en not_active Abandoned
- 1994-02-25 AU AU62067/94A patent/AU6206794A/en not_active Abandoned
- 1994-02-25 JP JP6518678A patent/JPH08509509A/en active Pending
- 1994-02-25 EP EP94909066A patent/EP0686180A1/en not_active Withdrawn
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2808412C1 (en) * | 2022-12-20 | 2023-11-28 | Акционерное общество "ТАИФ" | Method for processing heavy petroleum raw materials |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0686180A1 (en) | 1995-12-13 |
| WO1994019425A1 (en) | 1994-09-01 |
| AU6206794A (en) | 1994-09-14 |
| JPH08509509A (en) | 1996-10-08 |
| DE4306057A1 (en) | 1994-09-08 |
| DE4490891D2 (en) | 1997-07-31 |
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| Date | Code | Title | Description |
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| FZDE | Dead |