GB1601644A - Treatment of pyrolysis fuel oil - Google Patents
Treatment of pyrolysis fuel oil Download PDFInfo
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- GB1601644A GB1601644A GB20920/78A GB2092078A GB1601644A GB 1601644 A GB1601644 A GB 1601644A GB 20920/78 A GB20920/78 A GB 20920/78A GB 2092078 A GB2092078 A GB 2092078A GB 1601644 A GB1601644 A GB 1601644A
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- GB
- United Kingdom
- Prior art keywords
- fuel oil
- pyrolysis fuel
- liquid
- process according
- promoter
- Prior art date
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- 238000000197 pyrolysis Methods 0.000 title claims description 83
- 239000000295 fuel oil Substances 0.000 title claims description 78
- 239000007788 liquid Substances 0.000 claims description 63
- 238000000034 method Methods 0.000 claims description 35
- 238000004821 distillation Methods 0.000 claims description 23
- 239000011331 needle coke Substances 0.000 claims description 21
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 claims description 20
- 239000003921 oil Substances 0.000 claims description 20
- 238000000926 separation method Methods 0.000 claims description 16
- 239000006229 carbon black Substances 0.000 claims description 13
- 238000009835 boiling Methods 0.000 claims description 11
- 230000005484 gravity Effects 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000012512 characterization method Methods 0.000 claims description 10
- 238000004939 coking Methods 0.000 claims description 9
- 239000003350 kerosene Substances 0.000 claims description 8
- 239000003208 petroleum Substances 0.000 claims description 8
- 239000000571 coke Substances 0.000 claims description 5
- 239000010779 crude oil Substances 0.000 claims description 5
- 239000000047 product Substances 0.000 claims description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 4
- 239000005977 Ethylene Substances 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 239000005864 Sulphur Substances 0.000 claims description 4
- 239000006227 byproduct Substances 0.000 claims description 4
- 238000004230 steam cracking Methods 0.000 claims description 4
- 239000003502 gasoline Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 2
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 5
- 150000002790 naphthalenes Chemical class 0.000 description 4
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Chemical compound C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000002009 anode grade coke Substances 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- 239000011280 coal tar Substances 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical group CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 2
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 2
- 230000003111 delayed effect Effects 0.000 description 2
- DCAYPVUWAIABOU-UHFFFAOYSA-N hexadecane Chemical compound CCCCCCCCCCCCCCCC DCAYPVUWAIABOU-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000002791 soaking Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- IIYFAKIEWZDVMP-UHFFFAOYSA-N tridecane Chemical compound CCCCCCCCCCCCC IIYFAKIEWZDVMP-UHFFFAOYSA-N 0.000 description 2
- GQEZCXVZFLOKMC-UHFFFAOYSA-N 1-hexadecene Chemical compound CCCCCCCCCCCCCCC=C GQEZCXVZFLOKMC-UHFFFAOYSA-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
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000004996 alkyl benzenes Chemical class 0.000 description 1
- 229910021383 artificial graphite Inorganic materials 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- KWKXNDCHNDYVRT-UHFFFAOYSA-N dodecylbenzene Chemical compound CCCCCCCCCCCCC1=CC=CC=C1 KWKXNDCHNDYVRT-UHFFFAOYSA-N 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 229940078552 o-xylene Drugs 0.000 description 1
- 239000004711 α-olefin Substances 0.000 description 1
Classifications
-
- 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
- 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Carbon And Carbon Compounds (AREA)
- Coke Industry (AREA)
Description
(54) IMPROVEMENTS IN OR RELATING TO THE TREATMENT
OF PYROLYSIS FUEL OIL
(71) We, THE LUMMUS COMPANY, of 1515 Broad Street,Bloomfield, New Jersey 07003, United States of America, a company organised and existing under the Laws of the
State of Delaware, United States of America, do hereby declare the invention, for which we pray that a patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement This invention relates to the treatment of pyrolysis fuel oil and more particularly to a new and improved process for producing needle coke from a pyrolysis fuel oil (black oil).
Needle coke, after calcination and graphitisation, is characterised by a low longitudinal coefficient of thermal expansion which is matched by a low electric resistivity and such needle coke is primarily used in producing high quality synthetic graphite electrodes for electrosteel furnaces and for other electrothermal and chlor-alkali industries.
According to this invention, there is provided a process for treating a pyrolysis fuel oil containing asphaltenes, said pyrolysis fuel oil being a heavy residual black oil boiling above pyrolysis gasoline produced as by-product in the steam cracking of virgin petroleum fractions to ethylene, comprising: contacting said pyrolysis fuel oil with a petroleum fraction liquid promoter which enhances and promotes the separation of asphaltenes from said pyrolysis fuel oil, said liquid promoter have a5 volume percent distillation temperature of at least 310OF and a 95 volume percent distillation temperature of at least 350"F and no greater than 750"F, said liquid having a characterization factor of at least 9.75; and separating by gravity settling a liquid overflow of a pyrolysis fuel oil fraction having a reduced quantity of asphaltene, which is free of quinoline insolubles, from a liquid underflow of a pyrolysis fuel oil fraction having an increased quantity of asphaltene, said underflow and overflow including liquid promoter.
A fraction produced in this way may then be subjected to coking conditions of temperature and pressure to produce a needle coke or be employed directly for the production of carbon black.
The liquid which is employed to enhance and promote the separation of non-crystalline substances is generally a hydrocarbon liquid having a characterisation factor (K) of at least about 9.75 and preferably less than 12.0, wherein:
wherein Tn is the molal average boiling point of the liquid ("R); and G is specific gravity of the liquid (60"F/60"F).
The characterisation factor is an index of the aromaticity/paraffinicity of hydrocarbons and petroleum fractions as disclosed by Watson & Nelson Ind. Eng. Chem. 25 880 (1933), with more paraffinic materials having higher values for the characterisation factor (K). The promoter liquid which is employed is one which has a characterisation factor (K) in excess of 9.75.
The following Table provides representative characterisation factors (K) for various materials TABLE
Anthracene 8.3
Naphthalene 8.4 425-500"F Coar Tar Distillate 8.8 550-900"F Coal Tar Distillate 9.1 600-900"F Coal Tar Distillate 9.0 400-450"F Coal Tar Distillate 9.4
Benzene 9.8
Tetrahydronaphthalene 9.8
o-xylene 10,3 Decahydronaphthalene 10.6
Cyclohexane 11.0 425-500"F Boiling Range Kerosene 11.9
n-Dodecylbenzene 12.0
Propylene Oligomers (pentamer) 12.2
Cetene 12.8
Tridecane 12.8
n-Hexane 12.9
Hexadecane or cetane 13.0
The liquid which is used to enhance and promote the separation of non-crystalline substances preferably has a 5 volume percent distillation temperature of at least 4000F.The 95 volume percent distillation temperature is preferably no greater than 600"F. The most preferred promoter liquid has a 5 volume percent distillation temperature of at least 425"F and a 95 volume percent distillation temperature of no greater than 500"F. It is to be understood that the promoter liquid may be a single hydrocarbon; e.g., tetrahydronaphthalene, in which case the 5 volume percent and 95 volume percent distillation temperatures are the same; i.e., the hydrocarbon has a single boiling point. In such a case, the boiling point of the hydrocarbon must be at least 350"F in order to meet the requirement of a 5 volume percent distillation temperature of at least 310 F and a 95 volume percent distillation temperature of at least 3500F.The promoter liquid is preferably a blend or mixture of hydrocarbons in which case the 5 volume percent and 95 volume percent distillation temperatures are not the same.
The 5 volume percent and 95 volume percent distillation temperatures may be conveniently determined by ASTM No. D 86-67 or No. D 1160 with the former being preferred for those liquids having a 95 volume percent distillation temperature below 600"F and the latter for those above 600"F. The methods for determining such temperatures are well known in the art and further details in this respect are not required for a full understanding of the invention. It is also to be understood that the reported temperatures are corrected to atmospheric pressure.
As representative examples of such liquids, there may be mentioned: kerosene or kerosene fraction from paraffinic or mixed base crude oils; middle distillates, light gas oils and gas oil fractions from paraffinic or mixed based crude oils; alkyl benzenes with side chains containing ten or more carbon atoms; paraffinic hydrocarbons containing more than twelve carbon atoms; white oils or white oil fraction derived from crude oils; alphaolefins containing more than twelve carbon atoms; fully hydrogenated naphthalenes and substituted naphthalenes; propylene oligomers (pentamer and higher); tetrahydronaphthalene, heavy naphtha fractions, etc. The most preferred liquids are kerosene fractions; white oils; fully hydrogenated naphthalenes and substituted naphthalenes; and tetrahydronaphthalene.
The pyrolysis fuel oil or black oil (the two terms are used interchangeably to mean the residual heavy black oils boiling above pyrolysis gasolines which are produced as by-products in the steam cracking of virgin petroleum fractions to ethylene) is treated in accordance with the present invention to reduce the asphaltene content thereof in that such asphaltenes detract from the crystallinity of the needle coke product or the quality of carbon black to be produced therefrom.In treating pyrolysis fuel oils, it is generally not necessary to recover a fraction free of all asphaltenes in that some of the asphaltenes do not detract from the quality of the needle coke or carbon black product to be produced therefrom; accordingly, the promoter liquid can be employed to separate the asphaltenes which are most harmful to needle coke or carbon black quality, without separating all of the asphaltenes. Thus, the promoter liquid is added in an amount sufficient to reduce the asphaltene content of the pyrolysis fuel oil to thereby provide a pyrolysis fuel oil fraction of reduced asphaltene content suitable for the production of needle coke or carbon black. In general, the promoter liquid is employed in an amount to provide a promoter liquid to pyrolysis fuel oil weight ratio of from 0.3:1 to 5:1, and preferably of from 1:1 to 2:1.It is to be understood that the exact ratio will vary with the feedstock and promoter liquid.
Asphaltenes are separated from the pyrolysis fuel oil at a temperature in the order of from 50"C to about 300"C, and preferably at a temperature of from 100"C to 200"C. The separation can be effected at atmospheric pressure; however, higher pressures can be employed. The separation may be effected by any one of a wide variety of techniques, with gravity difference separation techniques being preferred, and gravity settling being particularly preferred. In employing gravity settling, a pyrolysis fuel fraction having a reduced content of asphaltenes is recovered as an overflow, and a pyrolysis fuel fraction with an increased content of asphaltenes is recovered as underflow.
In utilising the present invention, it has been found possible to recover a pyrolysis fuel oil fraction having an asphaltene content of no greater than 6%, and preferably no greater than 15tic, all by weight. In addition. the pyrolysis fuel oil fraction of reduced asphaltene content is generally recovered in a yield of at least 50%, and preferably at least 65%, based on pyrolysis fuel oil feed to the separation operation. The term "asphaltene" will be familiar to a man skilled in the Art, but is synonymous with the term "heptane insoluble" as measured by test No. 143-57 published by the Institute of Petroleum, London.
The pyrolysis fuel oil fraction treated in accordance with the present invention has been found generally to include some small amounts of quinoline insolubles and treatment in accordance with the invention also results in separation of such quinoline insolubles to provide a pyrolysis fuel oil fraction of reduced asphaltene content which is also free of quinoline insolubles.
The recovered treated pyrolysis fuel oil fraction, after separation of promoter liquid therefrom, may then be coked to a needle coke, preferably by a delayed coking technique, although other coking techniques are also possible.
The recovered pyrolysis fuel oil fraction containing an increased content of asphaltenes, after separation of promoter liquid therefrom, may also be coked to produce an anode grade coke. Alternatively, such fraction may be employed for coke oven charge blending, fuel or the like.
In one embodiment of the present invention, the treated recovered pyrolysis fuel oil fraction, having a reduced quantity of asphaltenes, can be soaked in the presence of sulphur. prior to coking, as described in U.S. Patent No. 3,687,840.
In order that the invention may be more readily understood, and so that further features thereof may be appreciated, the invention will now be described, by way of example, with reference to the accompanying drawing which is a simplified schematic flow diagram of an embodiment of the present invention.
Referring now to the drawing, a pyrolysis fuel oil in line 10 is combined with a liquid promoter in line 11. The liquid promoter is generally a hydrocarbon liquid having a characterisation factor (K) of at least 9.75 and preferably less than 12.0, wherein
wherein TB is the molal average boiling point of the liquid (OR); and G is specific gravity of the liquid (60"F/60"F). The combined stream in line 12 is introduced into a separation zone 13 in order to separate a pyrolysis fuel oil fraction of reduced asphaltene content from a pyrolysis fuel oil fraction of increased asphaltene content.As hereinabove noted, the separation zone 13 is preferably a gravity settling zone, containing one or more gravity settlers, whereby the pyrolysis fuel oil fraction of reduced asphaltene content is recovered as an overflow, with a pyrolysis fuel oil fraction of increased asphaltene content being recovered as an underflow.
The pyrolysis fuel oil fraction of reduced asphaltene content, which contains promoter liquid, is withdrawn from separation zone 13 through line 14 and is introduced into a fractionator, schematically indicated at 15, in order to recover the promoter liquid therefrom. An overhead of promoter liquid is withdrawn from fractionator 15 through line 16 combined with make-up in line 17 and recycled through line 11 for mixing with the pyrolysis fuel oil feed.
A pyrolysis fuel oil fraction of reduced asphaltene content is withdrawn from fractionator 15 through line 21 and introduced into a coker combination fractionating tower 22 of a type known in the art.
Preferably the pyrolysis fuel oil fraction is introduced into a sulphur soaking zone, schematically indicated as 23, as described in U.S. Patent Specification No. 3,687,840. The pyrolysis fuel oil is withdrawn from soaking zone 23 through line 24 for introduction into the cooker combination fractionator 22.
The coker combination fractionating tower 22 is operated as known in the art to recover a gas fraction, a distillate fraction, a light oil fraction, and a heavy oil fraction.
A cokeable bottoms product, having an initial boiling point of 290"C to 4300C is withdrawn from coker combination fractionating tower 22 through line 31 and passed through a coking heater 32 as known in the art wherein the fraction is heated to a temperature in the order of from about 4540C to about 515"C. The heated fraction in line 33 is introduced into a coking drum 34 wherein the fraction is delayed coked to needle coke.In general, as known in the art, such coking drums are operated at a pressure of from about 1.05 kglcm2 (g) to about 6.3 kg/cm2 (g), preferably from about 1.8 to 6.3 kg/cm2 (g), and at an overhead temperature of from about 414"C to about 475"C and preferably from about 460"C to about 475"C. The coke is withdrawn from the drum 34 through line 35.
An overhead is withdrawn from the coke drum 34 through line 36, and such overhead is introduced into the coker combination fractionator 22 to recover various fractions therefrom, as known in the art.
A pyrolysis fuel oil fraction, including an increased content of asphaltenes and promoter liquid is withdrawn from separation zone 13 through line 41 and introduced into a fractionator 42 to separate the promoter liquid therefrom. The separated promoter liquid is withdrawn from fractionator 42 as an overhead through line 43 for combination with the recycled promoter liquid in line 11.
A heavy pyrolysis fuel oil fraction is withdrawn from fractionator 42 and may be employed, for example. for the production of anode grade coke.
Alternatively, the heavy pyrolysis fuel oil fraction withdrawn through line 41 may be introduced through line 46 into a flash distillation zone, schematically indicated as 47, to recover the promoter liquid. as overhead through line 48, and a fraction boiling from about 315"C to about 538"C. as a sidestream through line 49, with the sidestream in line 49 being employed as additional feed for the production of needle coke.
The remaining heavy fraction, withdrawn as bottoms through line 51 may be employed for the production of, for example, anode grade coke.
The invention will be further described with respect to the following example Example
A pyrolysis fuel oil (18.2 wt.% asphaltenes; 0.09 wt. % Quinoline Insolubles) is mixed for 0.5 hr. at a temperature of 134"F with a promoter liquid having a characterisation factor of 11.8, a 5 volume percent distillation temperature of greater than 310 F and an end point of 425"F in an amount to provide a promoter liquid to pyrolysis fuel oil wt. ratio of 2.0:1.0.
The mixture is subjected to gravity settling (220"F; atmospheric pressure; 2.0 hrs) and the promoter liquid free overflow, contains 6.2 wt. % of asphaltenes and 0% quinoline insolubles and is recovered in a yield of 66.6 wt. %, based on pyrolysis fuel oil feed.
The recovered pyrolysis fuel oil fraction of reduced asphaltene content will produce a high grade of needle coke or a superior grade of carbon black.
Preferred embodiments of the present invention have been found to be particularly advantageous in that they make it possible to produce a high quality needle coke or carbon black in high yields. Thus, for example, high yields of needle coke or carbon black from pyrolysis fuel oil are made possible by the high recovery of non-distillable components having a reduced asphaltene content. Thus, in preferred embodiments of the present invention, it is possible to recover in excess of 65% of the non-distillable quinoline soluble components present in the pyrolysis fuel oil, having a reduced content of the asphaltenes which would interfere with the production of crystalline coke to thereby provide a feed suitable for the production of needle coke.
WHAT WE CLAIM IS:
1. A process for treating a pyrolysis fuel oil containing asphaltenes, said pyrolysis fuel oil being a heavy residual black oil boiling above pyrolysis gasoline produced as by-product in the steam cracking of virgin petroleum fractions to ethylene, comprising: contacting said pyrolysis fuel oil with a petroleum fraction liquid promoter which enhances and promotes the separation of asphaltenes from said pyrolysis fuel oil, said liquid promoter have a 5 volume percent distillation temperature of at least 3100F and a 95 volume percent distillation temperature of at least 3500F and no greater than 750"F, said liquid having a characterization factor of at least 9.75; and separating by gravity settling a liquid overflow of a pyrolysis fuel oil fraction having a reduced quantity of asphaltene, which is free of quinoline insolubles, from a liquid underflow of a pyrolysis fuel oil fraction having an increased quantity of asphaltene, said underflow and overflow including liquid promoter.
2. A process according to claim 1 wherein the promoter liquid is added in an amount to provide a promoter liquid to pyrolysis fuel oil weight ratio of from 0.3:1 to 5:1.
3. A process according to claim 1 or claim 2 wherein the promoter liquid has a 5 volume percent distillation temperature of at least 400"F and no greater than 600"F.
4. A process according to claim 3 wherein the said 5 volume percent distillation temperature is at least 425"F and the said 95 volume percent distillation temperature is no greater than 500"F.
5. A process according to any one of the preceding claims wherein the recovered pyrolysis fuel oil fraction contains at least 50% of the pyrolysis fuel oil.
6. A process according to any one of the preceding claims wherein at least a portion of the recovered pyrolysis fuel oil fraction is coked to needle coke.
7. A process according to claim 6 wherein the recovered fraction is heat soaked in the presence of sulphur prior to the coking.
8. A process according to any one of the preceding claims wherein the promoter liquid is kerosene, kerosene fractions, light gas oils, gas oil fractions, heavy naphthas, white oils and/or white oil fractions from crude oils.
9. A process according to any one of the preceding claims wherein the recovered pyrolysis fuel oil fraction has an asphaltene content of no greater than 6%, by weight.
10. A process according to any one of the preceding claims wherein at least a portion of the recovered pyrolysis fuel oil fraction is employed directly for the production of carbon black.
11. A process according to any one of claims 2 to 10 wherein the promoter liquid to pyrolysis fuel oil weight ratio is from 1:1 to 2:1.
12. A process for treating pyrolysis fuel oil substantially as herein described with reference to the accompanying drawing.
13. A process for treating pyrolysis fuel oil substantially as herein described with reference to the Example.
14. A product of a process according to any one of the preceding claims.
**WARNING** end of DESC field may overlap start of CLMS **.
Claims (14)
1. A process for treating a pyrolysis fuel oil containing asphaltenes, said pyrolysis fuel oil being a heavy residual black oil boiling above pyrolysis gasoline produced as by-product in the steam cracking of virgin petroleum fractions to ethylene, comprising: contacting said pyrolysis fuel oil with a petroleum fraction liquid promoter which enhances and promotes the separation of asphaltenes from said pyrolysis fuel oil, said liquid promoter have a 5 volume percent distillation temperature of at least 3100F and a 95 volume percent distillation temperature of at least 3500F and no greater than 750"F, said liquid having a characterization factor of at least 9.75; and separating by gravity settling a liquid overflow of a pyrolysis fuel oil fraction having a reduced quantity of asphaltene, which is free of quinoline insolubles, from a liquid underflow of a pyrolysis fuel oil fraction having an increased quantity of asphaltene, said underflow and overflow including liquid promoter.
2. A process according to claim 1 wherein the promoter liquid is added in an amount to provide a promoter liquid to pyrolysis fuel oil weight ratio of from 0.3:1 to 5:1.
3. A process according to claim 1 or claim 2 wherein the promoter liquid has a 5 volume percent distillation temperature of at least 400"F and no greater than 600"F.
4. A process according to claim 3 wherein the said 5 volume percent distillation temperature is at least 425"F and the said 95 volume percent distillation temperature is no greater than 500"F.
5. A process according to any one of the preceding claims wherein the recovered pyrolysis fuel oil fraction contains at least 50% of the pyrolysis fuel oil.
6. A process according to any one of the preceding claims wherein at least a portion of the recovered pyrolysis fuel oil fraction is coked to needle coke.
7. A process according to claim 6 wherein the recovered fraction is heat soaked in the presence of sulphur prior to the coking.
8. A process according to any one of the preceding claims wherein the promoter liquid is kerosene, kerosene fractions, light gas oils, gas oil fractions, heavy naphthas, white oils and/or white oil fractions from crude oils.
9. A process according to any one of the preceding claims wherein the recovered pyrolysis fuel oil fraction has an asphaltene content of no greater than 6%, by weight.
10. A process according to any one of the preceding claims wherein at least a portion of the recovered pyrolysis fuel oil fraction is employed directly for the production of carbon black.
11. A process according to any one of claims 2 to 10 wherein the promoter liquid to pyrolysis fuel oil weight ratio is from 1:1 to 2:1.
12. A process for treating pyrolysis fuel oil substantially as herein described with reference to the accompanying drawing.
13. A process for treating pyrolysis fuel oil substantially as herein described with reference to the Example.
14. A product of a process according to any one of the preceding claims.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US82573077A | 1977-08-18 | 1977-08-18 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| GB1601644A true GB1601644A (en) | 1981-11-04 |
Family
ID=25244787
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB20920/78A Expired GB1601644A (en) | 1977-08-18 | 1978-05-19 | Treatment of pyrolysis fuel oil |
Country Status (7)
| Country | Link |
|---|---|
| JP (1) | JPS5432502A (en) |
| CA (1) | CA1114764A (en) |
| DE (1) | DE2834475A1 (en) |
| FR (1) | FR2400548B1 (en) |
| GB (1) | GB1601644A (en) |
| IT (1) | IT1107957B (en) |
| NL (1) | NL184788C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2814467A1 (en) * | 2000-09-25 | 2002-03-29 | China Petroleum & Chemical | Combined multi-stage process of partial solvent de-asphalting and delayed coking of a charge by thermal cracking in the absence of hydrogen with fractionation of oil and vapour from the coking unit |
| US7846324B2 (en) | 2007-03-02 | 2010-12-07 | Exxonmobil Chemical Patents Inc. | Use of heat exchanger in a process to deasphalt tar |
| US8083931B2 (en) | 2006-08-31 | 2011-12-27 | Exxonmobil Chemical Patents Inc. | Upgrading of tar using POX/coker |
| US8083930B2 (en) | 2006-08-31 | 2011-12-27 | Exxonmobil Chemical Patents Inc. | VPS tar separation |
| US8709233B2 (en) | 2006-08-31 | 2014-04-29 | Exxonmobil Chemical Patents Inc. | Disposition of steam cracked tar |
| WO2017222742A1 (en) * | 2016-06-20 | 2017-12-28 | Exxonmobil Research And Engineering Company | Deasphalting and hydroprocessing of steam cracker tar |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4686027A (en) * | 1985-07-02 | 1987-08-11 | Foster Wheeler Usa Corporation | Asphalt coking method |
| EP2240554B1 (en) | 2008-01-28 | 2017-09-13 | Corina Projahn | Method and device to perform a pyrolysis |
| DE202008008767U1 (en) | 2008-06-27 | 2008-09-11 | Projahn, Corina | Apparatus for carrying out a pyrolysis |
| DE102008030983B4 (en) | 2008-06-27 | 2012-06-06 | Corina Projahn | Method and device for carrying out a pyrolysis and its use for smoldering waste tires and biomass |
| DE102008039817A1 (en) | 2008-08-22 | 2010-02-25 | Corina Projahn | Pyrolysis coke obtained by pyrolysis process, where the process after loading the furnace with pyrolyzable goods e.g. tires, comprises heating single or all heating element of the pyrolysis ovens, useful as e.g. heat insulating agent |
| CN104470994A (en) | 2012-05-17 | 2015-03-25 | W-Y·王 | Pyrolysis oil in carbon black production |
| DE102012109874A1 (en) | 2012-10-16 | 2014-04-17 | Merenas Trust Reg. | Apparatus and process for the material handling of raw materials |
| JP6553959B2 (en) * | 2015-06-23 | 2019-07-31 | 株式会社ブリヂストン | Carbon black, method for producing carbon black, rubber composition and tire |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE584763C (en) * | 1925-12-12 | 1933-10-16 | I G Farbenindustrie Akt Ges | Process for the processing of the products that arise when the coal is liquefied by hydrogenation |
| US2988501A (en) * | 1958-08-18 | 1961-06-13 | Union Oil Co | Hydrorefining of crude oils |
| US3326796A (en) * | 1964-06-22 | 1967-06-20 | Great Lakes Carbon Corp | Production of electrode grade petroleum coke |
| US3687840A (en) * | 1970-04-28 | 1972-08-29 | Lummus Co | Delayed coking of pyrolysis fuel oils |
| US3856675A (en) * | 1972-11-07 | 1974-12-24 | Lummus Co | Coal liquefaction |
| US3989803A (en) * | 1975-06-23 | 1976-11-02 | Phillips Petroleum Company | Concentration of carbonaceous solids in fuel oil stream in a carbon black procus |
-
1978
- 1978-05-19 GB GB20920/78A patent/GB1601644A/en not_active Expired
- 1978-07-24 CA CA307,976A patent/CA1114764A/en not_active Expired
- 1978-08-05 DE DE19782834475 patent/DE2834475A1/en active Granted
- 1978-08-10 IT IT50691/78A patent/IT1107957B/en active
- 1978-08-14 JP JP9897878A patent/JPS5432502A/en active Granted
- 1978-08-17 NL NLAANVRAGE7808537,A patent/NL184788C/en not_active IP Right Cessation
- 1978-08-17 FR FR7823992A patent/FR2400548B1/en not_active Expired
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2814467A1 (en) * | 2000-09-25 | 2002-03-29 | China Petroleum & Chemical | Combined multi-stage process of partial solvent de-asphalting and delayed coking of a charge by thermal cracking in the absence of hydrogen with fractionation of oil and vapour from the coking unit |
| US8083931B2 (en) | 2006-08-31 | 2011-12-27 | Exxonmobil Chemical Patents Inc. | Upgrading of tar using POX/coker |
| US8083930B2 (en) | 2006-08-31 | 2011-12-27 | Exxonmobil Chemical Patents Inc. | VPS tar separation |
| US8709233B2 (en) | 2006-08-31 | 2014-04-29 | Exxonmobil Chemical Patents Inc. | Disposition of steam cracked tar |
| US7846324B2 (en) | 2007-03-02 | 2010-12-07 | Exxonmobil Chemical Patents Inc. | Use of heat exchanger in a process to deasphalt tar |
| WO2017222742A1 (en) * | 2016-06-20 | 2017-12-28 | Exxonmobil Research And Engineering Company | Deasphalting and hydroprocessing of steam cracker tar |
| US10570342B2 (en) | 2016-06-20 | 2020-02-25 | Exxonmobil Research And Engineering Company | Deasphalting and hydroprocessing of steam cracker tar |
Also Published As
| Publication number | Publication date |
|---|---|
| NL184788C (en) | 1989-11-01 |
| DE2834475A1 (en) | 1979-03-01 |
| DE2834475C2 (en) | 1987-05-21 |
| FR2400548A1 (en) | 1979-03-16 |
| JPH0144272B2 (en) | 1989-09-26 |
| IT1107957B (en) | 1985-12-02 |
| JPS5432502A (en) | 1979-03-09 |
| NL7808537A (en) | 1979-02-20 |
| IT7850691A0 (en) | 1978-08-10 |
| CA1114764A (en) | 1981-12-22 |
| FR2400548B1 (en) | 1985-10-11 |
| NL184788B (en) | 1989-06-01 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PS | Patent sealed [section 19, patents act 1949] | ||
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 19950519 |