GB1031717A - Improvements in and relating to the hydrogenation of hydrocarbon oils - Google Patents
Improvements in and relating to the hydrogenation of hydrocarbon oilsInfo
- Publication number
- GB1031717A GB1031717A GB9478/62A GB947862A GB1031717A GB 1031717 A GB1031717 A GB 1031717A GB 9478/62 A GB9478/62 A GB 9478/62A GB 947862 A GB947862 A GB 947862A GB 1031717 A GB1031717 A GB 1031717A
- Authority
- GB
- United Kingdom
- Prior art keywords
- hydrocarbons
- gas
- chamber
- reaction
- hydrogen
- 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
Links
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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
-
- 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
- C10G2400/26—Fuel gas
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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
In a continuous process for the vapour phase hydrogenation of a hydrocarbon distillate oil comprising aliphatic constituents to obtain gaseous paraffinic hydrocarbons, wherein the oil vapour and a gas comprising hydrogen are continuously introduced into a thermallyinsulated reaction chamber so constructed as to define an endless path along which gas can circulate within the chamber, the oil vapour is reacted exothermically with hydrogen in the chamber at 600 DEG to 800 DEG C. at a pressure of at least 5 atmospheres gauge, gaseous products are continuously withdrawn from the chamber, the reactants are introduced in the form of at least one jet through orifice means into the reaction chamber to cause a substantial body of gas comprising reactants and products to circulate continuously around the said endless path, and the reactants are preheated to an extent such as to maintain a reaction temperature which is uniform throughout the reaction chamber except in the vicinity of the orifice means. Preferably, the reaction takes place at 700-800 DEG C. and 20 to 50 atmospheres gauge. The hydrogenating gas may be substantially wholly hydrogen but may also contain carbon monoxide or carbon dioxide, these mixtures being obtained by the reaction of coal coke or hydrocarbons with steam. The rate of deposition of carbon can be markedly decreased by incorporating steam into the hydrogenating gas, e.g. 10%. The expression "hydrocarbon distillate oils comprising aliphatic constituents" is used to refer to distillates consisting wholly or predominantly of hydrocarbons of which the aliphatic constituents are hydrocarbons or are the side chains of alkylated aromatic hydrocarbons. The term hydrocarbons includes both unsubstituted hydrocarbons and hydroxy substitution products of hydrocarbons, the hydroxyl groups of which are split off during the reaction. The hydrocarbon distillate oils may be petroleum distillates having boiling points in the range 160-360 DEG C., advantageusly light distillates having boiling points of from 70 DEG to 200 DEG C. Specified hydrocarbons are kerosene, butane, propane and coal tar distillates, e.g. creosote oils. To maintain the desired reaction temperature the oil vapour and hydrogenating gas are preheated to temperatures within the range 350 DEG to 550 DEG C. The ability of the gases to circulate in the reaction chamber is specified in terms of the recirculation ratio which is at least 3:1. The recirculation ratio is defined as the ratio of the volume of gas circulating within the reaction chamber to the volume of gas withdrawn from said chamber during one complete period of circulatory motion. In further preferred embodiments, 2 to 8 gallons of light distillate (measured as liquid distillate) are introduced with each 1000 cubic feet (measured at S.T.P.) of hydrogen in the hydrogenating gas, the temperature within the chamber, except in the vicinity of the inlet orifice is uniform to within \sB10 DEG C. and the velocity of introduction of the reactants is from 100 to 2,000 feet per second. As indicated in the Figure (not shown), hot hydrogenating gas is introduced into a reaction chamber until the temperature reaches 600 DEG C. at 25 atmospheres gauge. Oil vapour is then mixed with the hydrogenating gas and the composition of the mixture controlled to maintain the chamber temperature at 750 DEG C. The reaction gases circulate and products are taken off through an outlet. On analysis, the products contained a gaseous fraction, having 35% hydrogen, 49.3% methane, and 12.8% ethane, and a condensate containing benzene, toluene, naphthalene and higher aromatic hydrocarbons.
Priority Applications (9)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BE629454D BE629454A (en) | 1962-03-12 | ||
GB9478/62A GB1031717A (en) | 1962-03-12 | 1962-03-12 | Improvements in and relating to the hydrogenation of hydrocarbon oils |
DE19631470701 DE1470701A1 (en) | 1962-03-12 | 1963-03-11 | Vapor phase hydrogenation of hydrocarbon oils |
ES285937A ES285937A1 (en) | 1962-03-12 | 1963-03-11 | Continuous procedure for the hydrogenation in steam phase, of a distilled oil of hydrocarbons (Machine-translation by Google Translate, not legally binding) |
DK112263AA DK109102C (en) | 1962-03-12 | 1963-03-11 | Continuous process for the production of a gas containing methane or a mixture of methane and ethane. |
CH303163A CH467853A (en) | 1962-03-12 | 1963-03-11 | Continuous process for the hydrogenative splitting of distilled oils from a mixture of hydrocarbons |
AT196363A AT248593B (en) | 1962-03-12 | 1963-03-12 | Process for the continuous production of a combustible methane-rich gas |
JP38011448A JPS509801B1 (en) | 1962-03-12 | 1963-03-12 | |
FR927679A FR1350415A (en) | 1962-03-12 | 1963-03-12 | Process and apparatus for the hydrogenation of mineral oils and products according to those obtained |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB9478/62A GB1031717A (en) | 1962-03-12 | 1962-03-12 | Improvements in and relating to the hydrogenation of hydrocarbon oils |
Publications (1)
Publication Number | Publication Date |
---|---|
GB1031717A true GB1031717A (en) | 1966-06-02 |
Family
ID=9872746
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB9478/62A Expired GB1031717A (en) | 1962-03-12 | 1962-03-12 | Improvements in and relating to the hydrogenation of hydrocarbon oils |
Country Status (9)
Country | Link |
---|---|
JP (1) | JPS509801B1 (en) |
AT (1) | AT248593B (en) |
BE (1) | BE629454A (en) |
CH (1) | CH467853A (en) |
DE (1) | DE1470701A1 (en) |
DK (1) | DK109102C (en) |
ES (1) | ES285937A1 (en) |
FR (1) | FR1350415A (en) |
GB (1) | GB1031717A (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS58215484A (en) * | 1982-05-24 | 1983-12-14 | ブリテイツシユ ガス コ−ポレ−シヨン | Carbonic fuel hydrogenation |
WO1999046223A1 (en) * | 1998-03-09 | 1999-09-16 | Scott Specialty Gases, Inc. | Method and apparatus for direct fluorination of carbon or sulfur compounds |
-
0
- BE BE629454D patent/BE629454A/xx unknown
-
1962
- 1962-03-12 GB GB9478/62A patent/GB1031717A/en not_active Expired
-
1963
- 1963-03-11 DK DK112263AA patent/DK109102C/en active
- 1963-03-11 DE DE19631470701 patent/DE1470701A1/en active Pending
- 1963-03-11 ES ES285937A patent/ES285937A1/en not_active Expired
- 1963-03-11 CH CH303163A patent/CH467853A/en unknown
- 1963-03-12 AT AT196363A patent/AT248593B/en active
- 1963-03-12 JP JP38011448A patent/JPS509801B1/ja active Pending
- 1963-03-12 FR FR927679A patent/FR1350415A/en not_active Expired
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS58215484A (en) * | 1982-05-24 | 1983-12-14 | ブリテイツシユ ガス コ−ポレ−シヨン | Carbonic fuel hydrogenation |
WO1999046223A1 (en) * | 1998-03-09 | 1999-09-16 | Scott Specialty Gases, Inc. | Method and apparatus for direct fluorination of carbon or sulfur compounds |
Also Published As
Publication number | Publication date |
---|---|
AT248593B (en) | 1966-08-10 |
DK109102C (en) | 1968-03-18 |
BE629454A (en) | |
CH467853A (en) | 1969-01-31 |
DE1470701A1 (en) | 1969-06-19 |
FR1350415A (en) | 1964-01-24 |
ES285937A1 (en) | 1963-10-16 |
JPS509801B1 (en) | 1975-04-16 |
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