US3177262A - Production of naphthalene - Google Patents
Production of naphthalene Download PDFInfo
- Publication number
- US3177262A US3177262A US25531A US2553160A US3177262A US 3177262 A US3177262 A US 3177262A US 25531 A US25531 A US 25531A US 2553160 A US2553160 A US 2553160A US 3177262 A US3177262 A US 3177262A
- Authority
- US
- United States
- Prior art keywords
- hydrogen
- naphthalene
- mainly
- aromatic hydrocarbons
- temperature
- 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.)
- Expired - Lifetime
Links
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 title claims description 58
- 238000004519 manufacturing process Methods 0.000 title description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical class [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims description 33
- 239000001257 hydrogen Substances 0.000 claims description 33
- 238000006243 chemical reaction Methods 0.000 claims description 28
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 27
- 239000003208 petroleum Substances 0.000 claims description 22
- 229910052717 sulfur Inorganic materials 0.000 claims description 22
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 20
- 239000011593 sulfur Substances 0.000 claims description 20
- 238000009835 boiling Methods 0.000 claims description 18
- 229930195733 hydrocarbon Natural products 0.000 claims description 17
- 150000002430 hydrocarbons Chemical class 0.000 claims description 17
- 238000006900 dealkylation reaction Methods 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 14
- 238000000034 method Methods 0.000 claims description 14
- 239000007795 chemical reaction product Substances 0.000 claims description 12
- 230000020335 dealkylation Effects 0.000 claims description 12
- 239000004215 Carbon black (E152) Substances 0.000 claims description 10
- 230000003750 conditioning effect Effects 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 6
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 6
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 150000001875 compounds Chemical class 0.000 claims description 4
- 230000001143 conditioned effect Effects 0.000 claims description 4
- 238000007669 thermal treatment Methods 0.000 claims description 4
- JJCFRYNCJDLXIK-UHFFFAOYSA-N cyproheptadine Chemical compound C1CN(C)CCC1=C1C2=CC=CC=C2C=CC2=CC=CC=C21 JJCFRYNCJDLXIK-UHFFFAOYSA-N 0.000 claims 1
- 125000003118 aryl group Chemical group 0.000 description 25
- 229940075566 naphthalene Drugs 0.000 description 25
- 230000003197 catalytic effect Effects 0.000 description 10
- 238000004517 catalytic hydrocracking Methods 0.000 description 10
- 239000012141 concentrate Substances 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- 239000007788 liquid Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 239000000571 coke Substances 0.000 description 4
- 238000005336 cracking Methods 0.000 description 4
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 238000004523 catalytic cracking Methods 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000004227 thermal cracking Methods 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000011203 carbon fibre reinforced carbon Substances 0.000 description 2
- 230000001186 cumulative effect Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- KYYSIVCCYWZZLR-UHFFFAOYSA-N cobalt(2+);dioxido(dioxo)molybdenum Chemical compound [Co+2].[O-][Mo]([O-])(=O)=O KYYSIVCCYWZZLR-UHFFFAOYSA-N 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000000727 fraction Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 239000012808 vapor phase 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
Definitions
- This invention relates to the preparation of naphthalene from hydrocarbon stocks. It particularly relates to the method of producing naphthalene from petroleum fractions containing alkylnaphthalenes in admixture with other aromatic and/or non-aromatic hydrocarbons.
- Petroleum fractions which boil within the range of 400-550 F. generally contain substantial amounts of alkylnaphthalenes, such as mono-, di-, and .tri-methylnaphthalenes and in smaller quantity, the ethylnaphthw ,lenes.
- Recycle fractions which are formed in the cracking of petroleum stocks and which include this boiling range, often contain major proportions of aromatic hydrocarbons that are mainly alkylnaphthalenes. Such fractions typically may have aromatic contents varying within the range of 25-97% but usually contain between 50% and 95% aromatics depending upon the particular operation in which the petroleum fractions are produced.
- hydrocarbon charge stocks are obtained in both catalytic and thermal cracking processes and in operations in which combinations of catalytic and thermal cracking steps are utilized.
- Stock-s having high alkylnaphthalene contents can also be obtained by extracting straight run petroleum fractions of appropriate boiling ranges, such as kerosene, or catalytic fractions such as catalytic gas oil, with solvents, such as furfural or sulfur dioxide, or by selective adsorption with silica gel.
- These aromatic concentrates may contain 100% aromatic hydrocarbons.
- the present invention is directed to the use of hydrothe preparation of naphthalene in high concentration.
- the charge stock used in practicing the invention is a hydrocarbon fraction boiling substantially Within the range of 400-550" F. but more preferably between 450-- 550 F. and composed by weight of-35l00% aromatic hydrocarbons including substituted condensed ring aro matics such as alkylnaphth-alenes and from 65-0% nonaromatic hydrocarbons.
- This charge material also commonly contains substantial amounts of sulfur compounds that normally occur Within this boiling range.
- Charge stocks most typically employed have an aromatic content within the range of 50-95% by weight. In general, the substituted condensed ring aromatics constitute about 20% to 80% of the total aromatic hydrocarbons present in the charge stock.
- the present invention provides a method of making naphthalene from change stocks as specified above wherein the temperature rise due to the hydrocracking of the non-aromatics and the dealkylation of the aromatics is minimized and controlled.
- the charge material is first subjected to a conditioning treatment in the presence of a desulfurization catalyst and added hydrogen under conditions including a temperature within the range of 800- 980 F., at which the non-aromatic components are converted to lower boiling compounds at a slow enough rate to prevent excessive temperature rise. Under these conditions, substantial conversion of the alkylnaphthalenes into naphthalene does not occur.
- a minor proportion of the aromatic hydrocarbons are at least partially hydrogenated.
- the conditioned reaction product from this first step is then subjected in a second step to a temperature above 1000 .F., whereby deallrylation of the alkylnaphthalenes and dehydrogenation of the minor proportion of the aromatic hydrocarbons occurs.
- the temperature in this second stage reaction does not rise excessively. Furthermore, those aromatic hydrocarbons which were hydrogenated in the first step are dehydrogenated in the second step thereby additionally aiding in the temperature control of the second step due to the endothermic nature of the dehydrogenation reaction.
- the final reaction product is fractionated to obtain naphthalene in high concentration.
- the present invention is a two-stage process for making naphthalene from a hydrocarbon charge stock wherewith by removing the non-aromatics in the first stage and'by regulating the temperature in the first stage to vary the degree of aromatic saturation, it is possible to control the temperature rise during the second stage. Further, better temperature control is realized in the first stage with charge stocks containing non-aromatics since the exothermic addition of hydrogen to the aromatic hydrocarbons and to the cleaved carbon-carbon bonds tends to counterbalance the endothermic cracking of the nonaromatic hydrocarbons.
- the exothermic addition of hydrogen to the aromatic hydrocarbons provides additional heat so that the desired first stage temperature can be obtain-ed Without excessive external heat requirements.
- the endothermic dehydrogenation of the hydrogenated aromatics from the first stage reaction at least partially counterbalances the exothermic dealkylation reaction of the alkylnaphthalenes thereby providing better temperature control.
- hydrocracking primarily defined as the cumulative result of cleaving, i.e. cracking, carbon carbon bonds and of adding hydrogen to the cleaved bonds.
- the overall hydrocracking reaction is generally exother- 1111C.
- dealkylation is primarily defined: as the cumulative result of removing the alkyl side chains from the substituted condensed ring aromatic hydrocarbons and of adding hydrogen to form the 'dealkylated condensed
- the overall dealkylation reaction is generally exothermic.
- hydrocracking will also include the hydrogenation of a minor proportion of the aromatic hydrocarbonsand the term dealkylation will include the dehydrogenating of those aromatics hydrogenated during hydrocracking.
- the critical feature of the first stage reaction is to condition the first stage product by balancing hydrogenation, cracking, and desulfurization in such a manner that example, if the dicyclic aromatic is considered to be naphthalene, then the equilibrium relationship for-the reaction:
- naphthalene-i-Z hydrogenetetrahydronapthalene at 300 p.s.i.g. was found to be as follows.
- the hydrogen consumption under these conditions should be between 65-500 s.c.f. per barrel of liquid feed per percent sulfur in the feed and preferably between 200 and 400 -s.c.f./barrel. The.
- a still further manner practicing the invention involves catalyticallyconditioning the charge under the conditions set forth for the embodiment first mentioned above and then catalytically dealkylating the alkylnaphthalenes in the presence of a desulfurizationcatalyst.
- the presence of the catalyst in the latter. step facilitates the dealkylation reaction and in some-cases permits'it to be carried out at a lower temperature than that required for thermal dealkylation.
- the oatalyst also effects the conversion of any remaining sulfur into hydrogen sulfide and hence permits the preparation of naphthalene having negligible sulfur content.
- the conditions for the catalytic dealkylation step'in include a pressure of 150-1000 p.s.i.g.
- the first conditioning step is carried out in the-presence of a catalyst and added hydrogen while the second step involves a thermal treatment to effect dealkylation of the alky- V of the aromatic hydrocarbons is to be obtained.
- the total reaction product from the first conditioning step can be charged to the second step. However, it is-preferable to subject the first reaction product.
- distillation to distillation to obtain a fraction boiling mainly in the range of 400-550 -F. for use as charge to the second step.
- This distillation removes material formed in the first hydrocracking reaction which boilsbelow .400 F. and which will not contributeto the formation of naph thalene inthe second reaction stage... It also removes a minor amount of polymeric material that boils above 550 P. which would tend to contribute to coke formation if allowed to remain in the charge to thesecondstep.
- coking occurs after a time to such extent that coke removal from the reaction zone is required. This can 'be done in conventional manner by passing an oxygen-containing gas through the reaction zone to burn out the coke. In the steps inwhich a desulfurizing catalyst is used,.burning of coke from the catalyst restores its catalytic activity.
- a chargestock was prepared by distilling a gas oil fraction obtained by a combination or, catalytic and thermal cracking operations.
- the charge stock had a boiling range of 460-500 :F., an aromatic hydrocarbon content of 78% by weight, including about 1% naphthalene, and a sulfur content of.0.25 Hydrogen was mixed with the charge in a mole ratio of :1 and the mixture was heated to 900 F. and fed in vapor phase into a catalytic hydrocracking zone at a pressure of 500 p.s.i.g.
- Thecatalyst was a cobalt molybdate on alumina'desulfurizing catalyst containing 3% cobalt and molybdenum.
- the liquid space velocity of the charge in the reaction zone was 1 vol./vol. of catalyst/hr.
- the reaction product contained 8.3% of C -400 F. fraction having an F-l clear octane rating of 82.7 and 86.1% of material boiling above 400 F.
- the 400-450 F. fraction was composed predominantly of naphthalene and had a freezing point of 786 C. and a sulfur content of 0.06%.
- the higher boiling fraction contained a small amount of naphthalene due to imperfect fractionation.
- Overall yield of naphthalene, based on the original charge stock was 23.7%.
- Example III The charge stock prepared as in Example II was subjected to a conventional thermal hydrodealkylation treatment, omitting the first conditioning step of the invention.
- the charge stock' was admixed with hydrogen in a mole ratio of hydrogen to hydrocarbon of 10:1 under a pressure of 200 p.s.i.g. Heat was applied at a sufiicient rate to raise the temperature of the mixture to 1300 F. But beginning at a temperature of about 1125 F., the temperature rose rapidly to above 1600 F. before the reaction could be stopped. This was a characteristic runaway reaction.
- Example IV A catalytic gas oil was solvent extracted with furfural to prepare aromatic concentrates of varying aromatic contents. These aromatic concentrates were first subj'ected to catalytic conditioning and then thermal dealkylation. The results, indicating temperature control characteristics, are as follows:
- Samples C and D had 84% and 75% aromatic parting from the spirit of the invention.
- the temperature rise in the second stage was greater.
- Samples C and D had 84% and 75% aromatic parting from the spirit of the invention.
- undealkylated alkylnaphthalenes can be recycled to the process to effect greater yields.
- a two-stage process for making naphthalene from a sulfur-containing petroleum fraction boiling mainly within the range of 400* F. to 550 F. and composed of at least 50% aromatic hydrocarbons comprising mainly alkylnaphthalenes and the remainder comprising mainly non-aromatic hydrocarbons which comprises subjecting said petroleum fraction to conditioning treatment in the presence of a desulfurization catalyst and added hydrogen under reaction conditions including a temperature between 800 and 980 F.
- a two-stage process according to claim 4 where-in said petroleum fraction is selected from the group consisting of aromatic. concentrates separated from cracked gas oil and aromatic concentrates separated from straight run petroleum fractions.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US25531A US3177262A (en) | 1960-04-29 | 1960-04-29 | Production of naphthalene |
DE1443096A DE1443096C3 (de) | 1960-04-29 | 1961-04-17 | Verfahren zur Herstellung von Naphthalin aus Alkylnaphthallne enthaltenden Kohlenwasserstoffen |
LU40049D LU40049A1 (forum.php) | 1960-04-29 | 1961-04-22 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US25531A US3177262A (en) | 1960-04-29 | 1960-04-29 | Production of naphthalene |
Publications (1)
Publication Number | Publication Date |
---|---|
US3177262A true US3177262A (en) | 1965-04-06 |
Family
ID=21826620
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US25531A Expired - Lifetime US3177262A (en) | 1960-04-29 | 1960-04-29 | Production of naphthalene |
Country Status (3)
Country | Link |
---|---|
US (1) | US3177262A (forum.php) |
DE (1) | DE1443096C3 (forum.php) |
LU (1) | LU40049A1 (forum.php) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3260765A (en) * | 1965-05-25 | 1966-07-12 | Universal Oil Prod Co | Treatment of alkyl-substituted aromatic compounds |
US3284527A (en) * | 1963-12-31 | 1966-11-08 | Monsanto Co | Dealkylation of alkyl-substituted aromatics |
US3483266A (en) * | 1966-12-20 | 1969-12-09 | Monsanto Co | Thermal dealkylation of alkyl aromatic compounds employing a hydrogen donor and molecular hydrogen |
US3485883A (en) * | 1966-12-27 | 1969-12-23 | Monsanto Co | Dealkylation of alkyl aromatics using a hydrogenated aromatic hydrogen donor |
US3548019A (en) * | 1968-04-22 | 1970-12-15 | Sun Oil Co | Process for the production of naphthalene |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1999738A (en) * | 1928-01-13 | 1935-04-30 | Ig Farbenindustrie Ag | Purification of polynuclear aromatic hydrocarbons |
US2423176A (en) * | 1945-01-26 | 1947-07-01 | Shell Dev | Production of aromatic hydrocarbons |
US2577788A (en) * | 1949-07-26 | 1951-12-11 | Standard Oil Dev Co | Concurrent dealkylation of aromatic hydrocarbons and dehydrogenation of naphthenic hydrocarbons |
US3001932A (en) * | 1959-07-15 | 1961-09-26 | Exxon Research Engineering Co | Treatment of hydrocarbon oils |
-
1960
- 1960-04-29 US US25531A patent/US3177262A/en not_active Expired - Lifetime
-
1961
- 1961-04-17 DE DE1443096A patent/DE1443096C3/de not_active Expired
- 1961-04-22 LU LU40049D patent/LU40049A1/xx unknown
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1999738A (en) * | 1928-01-13 | 1935-04-30 | Ig Farbenindustrie Ag | Purification of polynuclear aromatic hydrocarbons |
US2423176A (en) * | 1945-01-26 | 1947-07-01 | Shell Dev | Production of aromatic hydrocarbons |
US2577788A (en) * | 1949-07-26 | 1951-12-11 | Standard Oil Dev Co | Concurrent dealkylation of aromatic hydrocarbons and dehydrogenation of naphthenic hydrocarbons |
US3001932A (en) * | 1959-07-15 | 1961-09-26 | Exxon Research Engineering Co | Treatment of hydrocarbon oils |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3284527A (en) * | 1963-12-31 | 1966-11-08 | Monsanto Co | Dealkylation of alkyl-substituted aromatics |
US3260765A (en) * | 1965-05-25 | 1966-07-12 | Universal Oil Prod Co | Treatment of alkyl-substituted aromatic compounds |
US3483266A (en) * | 1966-12-20 | 1969-12-09 | Monsanto Co | Thermal dealkylation of alkyl aromatic compounds employing a hydrogen donor and molecular hydrogen |
US3485883A (en) * | 1966-12-27 | 1969-12-23 | Monsanto Co | Dealkylation of alkyl aromatics using a hydrogenated aromatic hydrogen donor |
US3548019A (en) * | 1968-04-22 | 1970-12-15 | Sun Oil Co | Process for the production of naphthalene |
Also Published As
Publication number | Publication date |
---|---|
DE1443096C3 (de) | 1975-06-12 |
DE1443096A1 (de) | 1968-12-19 |
LU40049A1 (forum.php) | 1961-06-22 |
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