US2734809A - Method of making a fuel gas interchangeable with natural gas - Google Patents

Method of making a fuel gas interchangeable with natural gas Download PDF

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US2734809A
US2734809A US2734809DA US2734809A US 2734809 A US2734809 A US 2734809A US 2734809D A US2734809D A US 2734809DA US 2734809 A US2734809 A US 2734809A
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/20—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours
    • C10G11/22—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours produced by partial combustion of the material to be cracked

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  • This invention relates to a method of converting a hydrocarbon mixture, and preferably a normally liquid hydrocarbon mixture, into a fuel gas absolutely interchangeable with natural gas.
  • Another object of this invention is to provide a method of the nature indicated which can be operated continuously in simple relatively inexpensive apparatus.
  • the starting materials of the method of this invention are the gaseous and liquid paratfinic light petroleum fractions having a final boiling point up to about 500 F. These materials may also be characterized as having an average molecular carbon content ranging up to and including nine carbon atoms per molecule. Examples of such materials are propane, butane, hexane, heptane, octane, mixtures of aliphatic hydrocarbons up to and including pentadecane, natural gasoline, straight run gasoline and straight run naphtha. From the standpoint of economical storage, the preferred starting materials are those requiring no pressure or only a slight pressure, say, from five to ten pounds per square inch, on storage in liquid condition, for instance, natural gasoline.
  • a light hydrocarbon material is fed, as by means of a pump it), into a tube maintained at an elevated temperature within a cracking furnace 12.
  • the tube may be empty or may be filled with suitable refractory packing material. Steam may be added to control 'cracking'conditions. in this tube the hydrocarbon material is vaporized and cracked thermally to form a gaseous fraction and a vapor fraction made up predominantly of aromatic products which are separated from the gaseous products of the cracking step, for instance, in the manner illustrated in the flow sheet and described as follows:
  • the total products of the cracking step may be passed into the bottom portion of a first scrubber-condenser 14 made up of a vertical tube traversed longitudinally by a coil through which a cooling medium is circulated.
  • first scrubber-condenser is otherwise empty. Intermediate aromatic material in liquid form separated in a second scrubber-condenser 16 and cooled in a cooler 18 is sprayed into 14, as by means of a pump 20.
  • this first scrubbercondenser 14 an aromatic fraction (made up of heavy and intermediate aromatics such as tars, naphthalene and its derivatives, higher alkyl benzenes and the like) is separated in liquid form from the other products of the cracking step. This heavy aromatic fraction may be passed through a cooler 22 and thereafter recovered.
  • the remaining products of the cracking step (which remain in gaseous or vapor form) are passed into the bottom portion of the second scrubber-condenser 16 filled with suitable packing material.
  • a light aromatic fraction separated in liquid form in a condenser 24 is sprayed into the top of the second scrubber-condenser 16, as by means of a pump 26.
  • An intermediate aromatic fraction is separated in liquid form in the second condenser-scrubber 16 which, as disclosed, is sprayed into the first scrubber-condenser 14.
  • the cracking products left after the separation of the intermediate aromatic fraction pass into the condenser 24 and are there separated into a gas fraction and a liquid light aromatic fraction including benzene, toluene, xylenes and the like,
  • our method can be sub-divided into three steps, viz., initial thermal cracking (without catalyst), removal of non-gaseous cracking products, and passing the gaseous cracking products over a hydrogenation catalyst.
  • the gaseous cracking products contain both hydrogen and unsaturated hydrocarbons.
  • the catalyst chamber, the gaseous cracking products are autohydrogenated with formation of a product gas having reduced contents of hydrogen and unsaturated hydrocarbons and an increased parafiin content.
  • the substitute gas may have, but need not necessarily have, a chemical composition essentially similar to natural gas.
  • the burning characteristics of the substitute gas must be similar to natural gas.
  • the specific gravity and the heating value may differ from those of natural gas, as long as the value obtained by dividing the heating value by the square root of the specific gravity equals the value obtained in similar fashion from the corresponding characteristics of natural gas.
  • Natural gas may generally be characterized as free from hydrogen, from ethylene and from higher unsaturates; as
  • the cracking is conducted under specific, critically important pressure, residence time and temperature conditions to yield continuously a gas which at least when catalytically autohydrogenated is absolutely interchangeable with natural gas.
  • the pressure ismaintained, whenever' possible, at superatmospheric levels, say, at at least two atmospheres.
  • there is no upper limit for the pressure although as the pressure is increased, the yield of liquid products is raised at the expense of the yield of gas. Forthis reason, we prefer to operate at 3 to .4 atmospheres pressure, whenever possible.
  • the tempe'jrature is maintained at from 1300 to 1550 F.
  • the residence time may range from 10 to 2 seconds except in the cases specified in the next succeeding paragraph.
  • the residence time and the pressure are limited as follows.
  • the maximum pressures and residence times are, respectively, at less than 145 F.: 4 atmospheres and seconds; and at 1450 to 1550 F.: 3 atmospheres and 5 seconds.
  • the maximum pressure and residence time at 1450 to 1550 -F. are, respectively, 1 atmosphere and 3 to 4seconds and at less than 1450 5., respectively, 2 or 3 atmospheres and 5 seconds.
  • the cracking step will yield a gas containing from 12 to 15% ethylene, from 1 to 5% higher unsaturated hydrocarbons, from 10 to hydrogen, from 55 to 75% or more parafiins having an average carbon number ranging from 1.1 to 1.2 less than 2% nitrogen and other incombustibles and having a heating value of from 900 to 1250 B. t. u. per cubic foot as well as a specific gravity (air ,-1.000.) ranging from 0.55 to 0.78.
  • the liquid prodnets are low viscosity oils of from 7 to 40' A. P. I. containing from 60 to 80% light aromatics and boiling below 300 C.
  • the liquid products also include a heavy aromatic fraction. The amount of liquid products depends upon the starting material used and the pressure employed and may vary, for instance, from 4 to 40% of the total yield. Carbon deposition is negligible. Typical examples illustrating the nature of the gaseous and liquid products.
  • the autohydrogenation must be carried out catalytically at a temperature below 1200 F. and preferably at from 400 to 800 F. Best results are obtained at 500 to 700 F.
  • Super-atmospheric pressure is beneficial but not necessary.
  • the space velocity is maintained below 1000 cubic feet per cubic foot of catalyst volume per hour and may range as low as 200 cubic feet or less.
  • Any catalyst suitable forthe hydrogenation of unsaturated hydrocarbons may be used; for instance, iron, nickel, cobalt, the oxides of these metals, platinum, palladium, vanadium and its oxide, the oxides of chromium and molybdenum.
  • the catalytic autohydrogenation under the indicated conditions, of the gaseous products of the above described specific cracking step, yields a gas containing less than 5% ethylene when the feed gas contains approximately equal percentages of hydrogen andethylene.
  • the ethylene concentration may be reduced to 5 less than 1%.
  • hydrogen concentration may be reduced to less than 1%.
  • the combined hydrogen and ethylene concentration in the product gas will be below 15 while the concentration of parafitlns will above 80%, the paraflins having an average carbon number of from 1.1 to 1.3.
  • the product gas will have a heating value ranging from 1050 to 1150 B.
  • Gas A Gas B S ace velocity, S. 0. F40. F. catalyst/hour 300 250 v hlume ratio, make gas/teed gas 0.851 0. 915 Ethylene conversion, percent of ethylene- 93 87 Carbon balance, percent 101 100 Hydrogen balance, percent 98 101 Catalyst Temperature, F.:
  • Zone 1 595 670 Zone 2 565 705 Gas Composition Mol Percent COL.-- 0. 1 D. On. 0. 0 0. 0.0 0. 2.1 0. 5.
  • 0.1 0. 1. 1 2.
  • Aromatics 1.1 Heating value, 13. t. u./S. C. F.. 1,170 1, 14 Specific Gravity.(air 1.000) .72
  • the above disclosed process is characterized by a number of advantages.
  • the investment in equipment for storage of starting material (when using gasoline and naphtha) is quite low.
  • the product gas is absolutely interchangeable with natural gas.
  • the light aromatic fraction obtained as a by-product is readily marketed for solvent and chemical manufacture and as a motor fuel.
  • the heavy aromatic fraction obtained as another by-product can be burned to heat the cracking furnace and to generate steam.
  • a method for preparing a gas interchangeable with natural gas which comprises providing in vapor form a light paraflinic petroleum fraction having a final boiling point not in excess of 500 F., passing said vapor through a reactor maintained at a temperature of 1300 to 1550 F. and under a pressure of more than one atmosphere, the residence time in said reactor ranging from two to ten seconds, to thermally crack (without catalyst) said petroleum with the formation of a gas containing paraflins, olefins and hydrogen, separating the resulting product into a liquid fraction and a gaseous fraction and passing the gaseous fraction over a hydrogenation catalyst to effect autohydrogenation of said gas.
  • a continuous method for preparing a fuel gas interchangeable with natural gas characterized by minimum carbon deposition which comprises providing in vapor form an aliphatic hydrocarbon having a boiling point less than 500 F. and having the volatility of natural gasoline, passing said vapor through a reactor to thermally crack said vapor (without catalyst) while maintaining the temperature at from 1300 to 1550 F. and the residence time and pressure at values correlated with the temperature as tabulated:
  • a continuous method of preparing a fuel gas interchangeable with natural gas characterized by a minimum carbon deposition which comprises providing in vapor form an aliphatic hydrocarbon having a final boiling point of less than 500 F. and a volatility less than that of natural gasoline, passing said vapor through a reactor to thermally crack said vapor (without catalyst) while maintaining the temperature at from 1300 to 1550 F. and the residence time and pressure at values correlated with the temperature as tabulated:
  • Atmospheies 1,300 to 1,450 F 2 t0 5 2 t0 3 1,450 to 1,550 F 2 t0 4 to produce normally liquid products and a gas containing paraifins, olefins and hydrogen, separating the liquid fraction from the gas fraction, and passing the gas fraction over a hydrogenation catalyst to effect autohydrogenation of said gas.

Description

United States P METHOD OF MAKING A FUEL GAS INTER- CHANGEABLE WITH NATURAL GAS Application February 11, 1952, Serial No. 270,957 3 Claims. (Cl. 48-197) This invention relates to a method of converting a hydrocarbon mixture, and preferably a normally liquid hydrocarbon mixture, into a fuel gas absolutely interchangeable with natural gas.
With the increasing demand for gas as a premium fuel for domestic house heating, seasonal variation in gas sendout has been growing from year to year. To meet the resulting peak demands, it is desirable to produce and feed a substitute gas into the mains or pipelines. For this purpose, a method for making a substitute gas that is absolutely interchangeable with the normal sendout gas has long been desired but has heretofore not been available.
It is therefore an important object of the present invention to provide a method of preparing a fuel gas absolutely interchangeable with natural gas as prepared or, at the most, after admixture with the fuel gas of a small amount of an inert or diluent gas such asrair, nitro gen, carbon dioxide, combustion gas or the like.
Another object of this invention is to provide a method of the nature indicated which can be operated continuously in simple relatively inexpensive apparatus.
Other and further objects and features of this invention will become apparent from the following description and appended claims as illustrated by the accompanying drawing showing, diagrammatically and by way of example, apparatus for carrying out the method of this invention and the flow of material therethrough.
The starting materials of the method of this invention are the gaseous and liquid paratfinic light petroleum fractions having a final boiling point up to about 500 F. These materials may also be characterized as having an average molecular carbon content ranging up to and including nine carbon atoms per molecule. Examples of such materials are propane, butane, hexane, heptane, octane, mixtures of aliphatic hydrocarbons up to and including pentadecane, natural gasoline, straight run gasoline and straight run naphtha. From the standpoint of economical storage, the preferred starting materials are those requiring no pressure or only a slight pressure, say, from five to ten pounds per square inch, on storage in liquid condition, for instance, natural gasoline.
Referring now to the flow sheet of the drawing, a light hydrocarbon material is fed, as by means of a pump it), into a tube maintained at an elevated temperature within a cracking furnace 12. The tube may be empty or may be filled with suitable refractory packing material. Steam may be added to control 'cracking'conditions. in this tube the hydrocarbon material is vaporized and cracked thermally to form a gaseous fraction and a vapor fraction made up predominantly of aromatic products which are separated from the gaseous products of the cracking step, for instance, in the manner illustrated in the flow sheet and described as follows:
The total products of the cracking step may be passed into the bottom portion of a first scrubber-condenser 14 made up of a vertical tube traversed longitudinally by a coil through which a cooling medium is circulated. The
first scrubber-condenser is otherwise empty. Intermediate aromatic material in liquid form separated in a second scrubber-condenser 16 and cooled in a cooler 18 is sprayed into 14, as by means of a pump 20. In this first scrubbercondenser 14, an aromatic fraction (made up of heavy and intermediate aromatics such as tars, naphthalene and its derivatives, higher alkyl benzenes and the like) is separated in liquid form from the other products of the cracking step. This heavy aromatic fraction may be passed through a cooler 22 and thereafter recovered.
After separation of the heavy aromatic fraction (as described), the remaining products of the cracking step (which remain in gaseous or vapor form) are passed into the bottom portion of the second scrubber-condenser 16 filled with suitable packing material. A light aromatic fraction separated in liquid form in a condenser 24 is sprayed into the top of the second scrubber-condenser 16, as by means of a pump 26. An intermediate aromatic fraction is separated in liquid form in the second condenser-scrubber 16 which, as disclosed, is sprayed into the first scrubber-condenser 14. The cracking products left after the separation of the intermediate aromatic fraction pass into the condenser 24 and are there separated into a gas fraction and a liquid light aromatic fraction including benzene, toluene, xylenes and the like,
Thus broadly speaking, our method can be sub-divided into three steps, viz., initial thermal cracking (without catalyst), removal of non-gaseous cracking products, and passing the gaseous cracking products over a hydrogenation catalyst. The gaseous cracking products contain both hydrogen and unsaturated hydrocarbons. the catalyst chamber, the gaseous cracking products are autohydrogenated with formation of a product gas having reduced contents of hydrogen and unsaturated hydrocarbons and an increased parafiin content. i
Merely subjecting 'a starting material such as those indicated to thermal cracking followed by removal of nongaseous cracking products and autohydrogenation of gaseous cracking products does not necessarily yield a gas absolutely interchangeable with natural gas, as explained hereinbelow.
For such absolute interchangeability With natural gas, the substitute gas may have, but need not necessarily have, a chemical composition essentially similar to natural gas. The burning characteristics of the substitute gas must be similar to natural gas. To a limited extent, the specific gravity and the heating value may differ from those of natural gas, as long as the value obtained by dividing the heating value by the square root of the specific gravity equals the value obtained in similar fashion from the corresponding characteristics of natural gas. For a more complete discussion of the interchangeability of fuel gases with natural gas, reference is made to our copending application entitled Method of Preparing Fuel Gas Interchangeable with Natural Gas, filed February 11, 1952, now Patent No. 2,707,675.
Natural gas may generally be characterized as free from hydrogen, from ethylene and from higher unsaturates; as
Patented Feb. 14, 1956:
the top of the first scrubber-condenser and a vessel 30 filled with a hythe starting materials can be containing less than 15% of nitrogen and other incombustihles together with from 85% to 100% of paraffins having an average carbon number of from 1.0 to 1.3; as having a gross heating value ranging from 970 to 1200 B. t. u. per cubic foot and a specific gravity (air=1.000) ranging from 0.6 to 0.7; and as yielding a flame free from yellow tips or flash back.
According to the method of the present invention, the cracking is conducted under specific, critically important pressure, residence time and temperature conditions to yield continuously a gas which at least when catalytically autohydrogenated is absolutely interchangeable with natural gas.
' In producing an oil gas having a high paraitms to olefins ratio (which makes the gas easily subject to autohydrogenation yielding a fuel gas absolutely interchangeable with natural gas), the pressure ismaintained, whenever' possible, at superatmospheric levels, say, at at least two atmospheres. Apart from the limitations specified in the next following paragraph, there is no upper limit for the pressure, although as the pressure is increased, the yield of liquid products is raised at the expense of the yield of gas. Forthis reason, we prefer to operate at 3 to .4 atmospheres pressure, whenever possible. The tempe'jratureis maintained at from 1300 to 1550 F. The residence time may range from 10 to 2 seconds except in the cases specified in the next succeeding paragraph.
To maintain the carbon deposition not above 2 /2 weight per cent of the material being cracked (whereby continuous cracking can be carried out for 24 hours or longer), the residence time and the pressure are limited as follows. Inthe case of a material of the volatility of natural gasoline, the maximum pressures and residence times are, respectively, at less than 145 F.: 4 atmospheres and seconds; and at 1450 to 1550 F.: 3 atmospheres and 5 seconds. In the case of material less volatile than natural gasoline and not less volatile than straight run naphtha, the maximum pressure and residence time at 1450 to 1550 -F. are, respectively, 1 atmosphere and 3 to 4seconds and at less than 1450 5., respectively, 2 or 3 atmospheres and 5 seconds.
For normal operating conditions within the indicated limits, the cracking step will yield a gas containing from 12 to 15% ethylene, from 1 to 5% higher unsaturated hydrocarbons, from 10 to hydrogen, from 55 to 75% or more parafiins having an average carbon number ranging from 1.1 to 1.2 less than 2% nitrogen and other incombustibles and having a heating value of from 900 to 1250 B. t. u. per cubic foot as well as a specific gravity (air ,-1.000.) ranging from 0.55 to 0.78. The liquid prodnets are low viscosity oils of from 7 to 40' A. P. I. containing from 60 to 80% light aromatics and boiling below 300 C. The liquid products also include a heavy aromatic fraction. The amount of liquid products depends upon the starting material used and the pressure employed and may vary, for instance, from 4 to 40% of the total yield. Carbon deposition is negligible. Typical examples illustrating the nature of the gaseous and liquid products.
when, cracking naphthas within the specified range of conditions are given hereinbelow.
The autohydrogenation must be carried out catalytically at a temperature below 1200 F. and preferably at from 400 to 800 F. Best results are obtained at 500 to 700 F. Super-atmospheric pressure is beneficial but not necessary. The space velocity is maintained below 1000 cubic feet per cubic foot of catalyst volume per hour and may range as low as 200 cubic feet or less. Any catalyst suitable forthe hydrogenation of unsaturated hydrocarbons may be used; for instance, iron, nickel, cobalt, the oxides of these metals, platinum, palladium, vanadium and its oxide, the oxides of chromium and molybdenum.
The catalytic autohydrogenation, under the indicated conditions, of the gaseous products of the above described specific cracking step, yields a gas containing less than 5% ethylene when the feed gas contains approximately equal percentages of hydrogen andethylene. When there is-a considerable excess of hydrogen (over the ethylene) in the feed gas, the ethylene concentration may be reduced to 5 less than 1%. Conversely, in the instance of a higher concentration of ethylene than hydrogen in the feed gas, hydrogen concentration may be reduced to less than 1%. Normally, the combined hydrogen and ethylene concentration in the product gas will be below 15 while the concentration of parafitlns will above 80%, the paraflins having an average carbon number of from 1.1 to 1.3. The product gas will have a heating value ranging from 1050 to 1150 B. t. 11. per cubic foot as well as a specific gravity (air=1.000) ranging from 0.6 to 0.7. This productgas has the same burning characteristics as natural gas and is therefore absolutely interchangeable therewith. Insome instances, a small amount of air, nitrogen, combustion gas or the like diluent, incombustible or inert gas can be blended with the product gas to match a natural gas containing a considerable percentage of incombustible gas. If desired, an inert or incombustible diluent gas may be added ahead of the cracking step.
The following examples will illustrate the working of the method of this invention. In the three examples, naphthas were cracked at 3 atmospheres total pressure, a temperature of 1500 F. and residence times of 4.3 and 4.6 seconds.
The make gases were found, to have the characteristics tabulated as follows:
Residence Time 4.3 Sec. 4.6 See.
Gas Composition, Mol Percent:
C0: 0. 0 0. 0 O2... 0. 0 0. 0 CO 0.0 0. 0 N2. 1. 8 0. 2 HL 20. 3 18. 9 CH4... 55. 2 56. 9 0211 5. 6 5. 4 O H5.-.. 0. 0 0. 4 C4 1u- 0. 0 0. 0 02H 13. 5 l5. 4 051% 1. 3 1. 5 C413 0. 3 0. 3 -5H1u 0. 0 0. 0 Diolefins and acetylene 0. 5 0.5 Aromatics 0.9 0. 5 Heating value, B. t. u./S. O. F-.. 1, 023 1,080 Specific gravity (air =1.000) 0. 61 0. 63
The above gases (identified hereinbelow as Gas A and Gas B) were autohydrogenated under difierent conditions. In both cases,.we used a nickel oxide catalyst precipitated on kieselguhr containing 10%. elemental nickel. The operating conditions and product gas com positions are tabulated as follows:
Gas A Gas B S ace velocity, S. 0. F40. F. catalyst/hour 300 250 v hlume ratio, make gas/teed gas 0.851 0. 915 Ethylene conversion, percent of ethylene- 93 87 Carbon balance, percent 101 100 Hydrogen balance, percent 98 101 Catalyst Temperature, F.:
Zone 1 595 670 Zone 2 565 705 Gas Composition, Mol Percent COL.-- 0. 1 D. On. 0. 0 0. 0.0 0. 2.1 0. 5. 4 11. 65. 7 64. 22.0 16. 1. 4 1. 0.1 0. 1. 1 2. 0. 'i l. 0.0 0. 0.1 0. 0. 0 Aromatics 1.1 Heating value, 13. t. u./S. C. F.. 1,170 1, 14 Specific Gravity.(air=1.000) .72
Both gases were found to be absolutely interchangeable with natural gas. Practically identical results were obtained by cracking and then catalytically autohydrogenating butane, propane, and straight run and natural gasoline.
The above disclosed process is characterized by a number of advantages. The investment in equipment for storage of starting material (when using gasoline and naphtha) is quite low. The product gas is absolutely interchangeable with natural gas. The light aromatic fraction obtained as a by-product is readily marketed for solvent and chemical manufacture and as a motor fuel. The heavy aromatic fraction obtained as another by-product can be burned to heat the cracking furnace and to generate steam.
Many details of construction may be varied within a wide range and it is therefore not our intention to limit the patent granted on this invention otherwise than necessitated by the scope of the appended claims.
This application is a continuation-in-part of application Serial No. 185,274, filed September 16, 1950, entitled Method of Making a Calorific Gas Interchangeable with Natural Gas.
We claim:
1. A method for preparing a gas interchangeable with natural gas which comprises providing in vapor form a light paraflinic petroleum fraction having a final boiling point not in excess of 500 F., passing said vapor through a reactor maintained at a temperature of 1300 to 1550 F. and under a pressure of more than one atmosphere, the residence time in said reactor ranging from two to ten seconds, to thermally crack (without catalyst) said petroleum with the formation of a gas containing paraflins, olefins and hydrogen, separating the resulting product into a liquid fraction and a gaseous fraction and passing the gaseous fraction over a hydrogenation catalyst to effect autohydrogenation of said gas.
2. A continuous method for preparing a fuel gas interchangeable with natural gas characterized by minimum carbon deposition which comprises providing in vapor form an aliphatic hydrocarbon having a boiling point less than 500 F. and having the volatility of natural gasoline, passing said vapor through a reactor to thermally crack said vapor (without catalyst) while maintaining the temperature at from 1300 to 1550 F. and the residence time and pressure at values correlated with the temperature as tabulated:
to produce normally liquid products and a gas containing parafiins, olefins and hydrogen, separating the liquid fraction from the gas fraction and passing the gas fraction over a hydrogenation catalyst to effect autohydrogenation of said gas.
3. A continuous method of preparing a fuel gas interchangeable with natural gas characterized by a minimum carbon deposition which comprises providing in vapor form an aliphatic hydrocarbon having a final boiling point of less than 500 F. and a volatility less than that of natural gasoline, passing said vapor through a reactor to thermally crack said vapor (without catalyst) while maintaining the temperature at from 1300 to 1550 F. and the residence time and pressure at values correlated with the temperature as tabulated:
Time, Pressure Temperature Seconds Atmospheies 1,300 to 1,450 F 2 t0 5 2 t0 3 1,450 to 1,550 F 2 t0 4 to produce normally liquid products and a gas containing paraifins, olefins and hydrogen, separating the liquid fraction from the gas fraction, and passing the gas fraction over a hydrogenation catalyst to effect autohydrogenation of said gas.
References Cited in the file of this patent UNITED STATES PATENTS OTHER REFERENCES Sachanen: Conversion of Petroleum, 2nd ed., page 211, New York, Reinhold Publishing Corp., 1948.
Production of Manufacture Gas Using Turbine Cycles, April 1948.

Claims (1)

1. A METHOD FOR PREPARING A GAS INTERCHANGEABLE WITH NATURAL GAS WHICH COMPRISES PROVIDING IN VAPOR FORM A LIGHT PARAFFINIC PETROLEUM FRACTION HAVING A FINAL BOILING POINT NOT IN EXCESS OF 500* F., PASSING SAID VAPOR THROUGH A REACTOR MAINTAINED AT A TEMPERATURE OF 1300 TO 1550* F. AND UNDER A PRESSURE OF MORE THAN ONE ATMOSPHERE, THE RESIDENCE TIME IN SAID REACTOR RANGING FROM TWO TO TEN SECONDS, TO THERMALLY CRACK (WITHOUT CATALYST) SAID PETROLEUM WITH THE FORMATION OF A GAS CONTAINING PARAFFINS,
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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2910428A (en) * 1957-04-01 1959-10-27 Exxon Research Engineering Co Upgrading light virgin naphtha
US2956093A (en) * 1958-02-25 1960-10-11 Exxon Research Engineering Co Olefin and town gas production
DE1175819B (en) * 1960-08-13 1964-08-13 Azote Office Nat Ind Process for producing a gas that can be used instead of natural gas from heavier hydrocarbons than methane and ethane
US3421870A (en) * 1964-02-17 1969-01-14 Exxon Research Engineering Co Low-temperature catalytic hydrogen-olysis of hydrocarbons to methane
US3942957A (en) * 1973-05-14 1976-03-09 British Gas Corporation Production of combustible gases
US4065514A (en) * 1972-07-17 1977-12-27 Texaco Inc. Preparation of methane
EP2014743A1 (en) * 2007-06-25 2009-01-14 Ineos Europe Limited Autothermal cracking process for producing olefins
US20120041242A1 (en) * 2010-08-12 2012-02-16 Gregory Joseph Panuccio Substitute natural gas generation

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DE531430C (en) * 1928-04-03 1931-08-10 Hermann Blau Extraction of liquid luminous gas and gaseous engine fuel for airships from the pyrogenic fission products of mineral oils
US2097489A (en) * 1934-02-01 1937-11-02 Stephen A Kiss Process of gasifying oils and coals
US2154676A (en) * 1937-09-20 1939-04-18 Ig Farbenindustrie Ag Production of ethylene from saturated hydrocarbons
US2283643A (en) * 1938-09-10 1942-05-19 Nagel Theodore Making gas from oil
US2340814A (en) * 1940-04-02 1944-02-01 Rex E Lidov Process for converting hydrocarbon oils
US2605176A (en) * 1949-09-02 1952-07-29 Allied Chem & Dye Corp Manufacture of combustible gas
US2608478A (en) * 1946-02-01 1952-08-26 Phillips Petroleum Co Production of fuel gas by cracking propane

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE531430C (en) * 1928-04-03 1931-08-10 Hermann Blau Extraction of liquid luminous gas and gaseous engine fuel for airships from the pyrogenic fission products of mineral oils
US2097489A (en) * 1934-02-01 1937-11-02 Stephen A Kiss Process of gasifying oils and coals
US2154676A (en) * 1937-09-20 1939-04-18 Ig Farbenindustrie Ag Production of ethylene from saturated hydrocarbons
US2283643A (en) * 1938-09-10 1942-05-19 Nagel Theodore Making gas from oil
US2340814A (en) * 1940-04-02 1944-02-01 Rex E Lidov Process for converting hydrocarbon oils
US2608478A (en) * 1946-02-01 1952-08-26 Phillips Petroleum Co Production of fuel gas by cracking propane
US2605176A (en) * 1949-09-02 1952-07-29 Allied Chem & Dye Corp Manufacture of combustible gas

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2910428A (en) * 1957-04-01 1959-10-27 Exxon Research Engineering Co Upgrading light virgin naphtha
US2956093A (en) * 1958-02-25 1960-10-11 Exxon Research Engineering Co Olefin and town gas production
DE1175819B (en) * 1960-08-13 1964-08-13 Azote Office Nat Ind Process for producing a gas that can be used instead of natural gas from heavier hydrocarbons than methane and ethane
US3421870A (en) * 1964-02-17 1969-01-14 Exxon Research Engineering Co Low-temperature catalytic hydrogen-olysis of hydrocarbons to methane
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