US2605176A - Manufacture of combustible gas - Google Patents

Manufacture of combustible gas Download PDF

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US2605176A
US2605176A US113765A US11376549A US2605176A US 2605176 A US2605176 A US 2605176A US 113765 A US113765 A US 113765A US 11376549 A US11376549 A US 11376549A US 2605176 A US2605176 A US 2605176A
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Prior art keywords
zone
gas
downwardly
riser pipe
empty
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US113765A
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English (en)
Inventor
Harry B Pearson
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Honeywell International Inc
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Allied Chemical and Dye Corp
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Publication date
Priority to BE497277D priority Critical patent/BE497277A/xx
Application filed by Allied Chemical and Dye Corp filed Critical Allied Chemical and Dye Corp
Priority to US113765A priority patent/US2605176A/en
Priority to GB16000/50A priority patent/GB683564A/en
Priority to FR1022014D priority patent/FR1022014A/fr
Priority to DEA3069A priority patent/DE847945C/de
Application granted granted Critical
Publication of US2605176A publication Critical patent/US2605176A/en
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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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C10G9/38—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours produced by partial combustion of the material to be cracked or by combustion of another hydrocarbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/14—Production of inert gas mixtures; Use of inert gases in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/16—Continuous processes simultaneously reacting oxygen and water with the carbonaceous material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1253—Heating the gasifier by injecting hot gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • This invention relates to the manufacture of fuel gas from hydrocarbons and. more particularly refers to a new and. improved process and apparatus for converting normally liquid hydrocarbon oils and condensible hydrocarbon gases referred to in the industry as L. P. gas or liquidpetroleum gas which gases include propane, butane and pentane into a highly combustible homogeneous gas of'a quality adapted to be principally used for heating.
  • L. P. gas or liquidpetroleum gas which gases include propane, butane and pentane into a highly combustible homogeneous gas of'a quality adapted to be principally used for heating.
  • the oil cracking apparatus should be flexible particularly in its ability to treat less costly fractions of petroleum oils such as low gravity gas oils or heavy residuums and also in its capability of changing the properties of the gas product within reasonable limits and its rate of production without seriously impairing the operation. Since price is a dominant factor controlling the sale of fuel gas over other competitive fuels all elements entering into the cost of the gas such as investment cost, value of charging stock, operating cost, maintenance and yield are of paramount importance to the manufacturer. In view of the high volume of gases consumed, small differentials in price per 1000 cu. ft. of heating gas which may appear insignificant, when multiplied by the total output of the gas in millions of cu. ft. assume substantial proportions in dollars. Furthermore, oil cracking machines should not only be simple and efiicient in operation but also compact in design.
  • the quality of a heating gas is, of course, governed by the consumers" requirements.
  • the greatest number of customers of gas burn gas in atmospheric gas burners fixed in the sense of having orifices of a definite size and air shutters open to a predetermined extent which cannot conveniently be changed thereby imposing on the gas producer the necessity for maintaining a uniform quality of gas.
  • Other important considerations in the efiicient operation of atmospheric burners are the properties'of the gas, particularly the calorific value and density of the gas.
  • a gas should have a B. t. u. per cu. ft.
  • anoil gas having these characteristics being hereinafter designated as high B. t. u. low gravity gas.
  • the density of a gas is influenced to alar egdegree by its content of hydrogen and illuminants, i. e. hydrocarbons of higher molecular weight. Gases containing too large a volume of hydrogen tend to flashback and gases haVingQtoo large a percentage of illuminant's give anl'elongated flame. To my knowledge none of the prior art oil cracking de- -vices'has succeeded.fin coinmercially producing high B. t. u. low gravity gas.
  • a further object of the invention is to provide an oil gas apparatus simple in construction, compact in design, and durable, certain and efficient in operation.
  • a still further object of this invention is to provide an improved process and apparatus for decomposing hydrocarbon oils into gas which is economical, elastic and flexible in operation.
  • Apparatus for carrying .out the conversion .of oil into gas in accordance with :the. present invention involves a novel combination and arrangement .of elements including two vertical refractory lined duplicate vessels connected at their tops by asgasrchannel, each vessel constructed to provide an empty chamber above another chamber at least partially filled with checkerbrick or refractory material with voids therebetween to permit the passage of gas therethrough and divided therefrom by a refractory circular orifice, two vertical refractory lined riser pipes'extending upwardly :to a height above the vessels with each riser pipe connected to the base of a refractory ifilled chamber, a stack valve fitted to the top of ..each riser pipe, conduits leading from .the top .of each ,riser pipe :connected to a three-way valve for reversal of flow in the apparatus and for the release of make gas, an inlet for the introduction :of primary air into each riser pipe, a steam conduit leading into each riser pipe, .a gas
  • plete cycle of operation comprises, (a) a blast lhe operation .ofemy process involves passing 7 air upwardly through a first zone at least partially filled with heated refractory material with voids therebetween'to permit the passage,
  • This I accomplish by first heating the empty chamber to a peak cracking temperature of the system and then injecting hydrocarbon oil into the heated empty chamber countercurrent to an upward flow of a mixture of steam and hydrocarbon carrier gas introduced into the bottom of the empty chamber at a velocity high enough to prevent the oil and carbonaceous materials from flowing down through the chamber.
  • the combination of upwardly flowing steam and hydrocarbon gas and peak temperature in the empty chamber causes vaporization and cracking of the liquid oil with concomitant production of carbon and carbonaceous material which deposit on the walls of the empty chamber leaving effluent vapors and gas substantially free from solid carbonaceous material and liquid oil for'further conversion, i. e. fixing, in a separate zone.
  • Confining the bulk of the carbonaceous material to the walls of an empty chamber is beneficial in that the flow of materials through the apparatus is not materially impeded, thus maintaining high throughput as well as reducing shut-downs for cleaning. Furthermore, avoidance of material deposition of carbonaceous material on the checkerbrick eliminates rapid deterioration of the brickwork which normally requires frequent replacement, due, it is believed, to thermal shock resulting from direct impingement of the carbon on the checkerbrick and the burning of the carbon from g the checkerbrick causing localized hot spots.
  • hydrocarbon carrier gas to the steam during the make period has manifold advantages. It supplements the steam as a propelling agent for carryingthe oil vapors through the apparatus. It aids "inqpreventing oilv and carbonaceous material from dropping 'down through the bottom of the empty chamber. It
  • portions of the oil are overcracked with the deposition of excess carbon and other portions of the oil are undercracked with incomplete uti lization of the oil.
  • more favorable temperature conditions in the cracking zone may be attained by blasting upwardly through an empty reaction zone to a peak gas making temperature and then passing combustion gases downwardly through another empty.
  • the downward flow of gases through the empty reaction zone and checkerbrick section of the fix ing zone gives a relatively even downward temperature gradient following the path of combustion gases and a more uniform heat distribution throughout the checkerbrick section.
  • the introduction of a hydrocarbon carrier gas during the make period has the cumulative effect of better distribution of the oil thereby also mini- 5O mizing overcracking and undercracking.
  • the accompanying drawing is a diagrammatic fiow sheet illustrating the apparatus and process of the present invention.
  • terials 3 which refractoryJining absorbs heat and also protects the metal shell 2 which sur rounds it from the direct impact of hot gases.
  • insulation may be interposcdbetween shell 2 and refractory lin ing Vessel I is divided'into two sectiona'an empty upper reaction chamber i'and a lower preheating or fixing chamber 5 filled with a refractory material 6 wherein will be retained and stored up surplus heat and which will give up heat.
  • Dividing reaction chamber i and fixing chamber 5 is a circular orifice lwhich has the function of effecting thorough' mixing of the gases and also imparting a high velocity to the gas entering the bottom of chambers
  • a refractory lined conduit 8 connects the bottom of vessel 1 with the bottom of refractory lined riser pipe 8 which extends upwardly to a height, suitable to carry the blast gases above other equipment and to provide draught when the set is. shut down.
  • a stack valve I l is fitted to the top of riser pipe 9 and disposed above it is stack 12. Make gas discharges from the top of riser pipe 9 through line i3 connected to a conventional three-way reversing valve l4. Primary air introduced for example by a blower, not shown in the drawing, enters,
  • Steam may be introduced into riser pipe 9 through line I8 and valve 19.
  • Hydrocarbon carrier gas from an external source joins the flow of steam entering through line 65, valve -29 and entrance 2!, preferably disposed at the. bottom of riser pipe 9 V
  • recycle make gas is returned as thecarrier agent to the bottom of preheating chamber-5 through line 56,
  • Make oil is fed throughlines 2 2, 23, valve 24 and sprayed downwardly'by means of nozzle 25, of conventional design; counter-current to the upward flow of gases in reaction chamber 5.
  • Heat oil passes through line 26, 21, valve 23 into reaction chamber 4 through nozzle 29.
  • a'carrier gas- may be dispcnsed with entirely and'steam in the absence of event no make gas would be recycled or make gas returned only during a part of the make time.
  • No. 2 set and No. 1 set are substantially duplicates, the corresponding elements of set No. 2 bearing the following numerals: Vessel 35, metal shell 36, refractory lining 3?, reaction chamber 38, fixing chamber 3Q,.checkerbrick 3i, orifice 42, riser pipe 43, connecting conduit 4 stack valve G5, stack 46, steam inlet and valve ii? and 38, respectively, hydrocarbon carrier gas inlet and valve 49 and 50, hydrocarbon carrier gas con duit from an external source 653, recycle line, valve, exhauster I I, 12 and i3, respectively, primary air inlet and valve 52 and 55, respectively, secondary air inlet and valve 54 and 55, respectively, make oil line, valve and nozzle 5? and 53, respectively, heat oil line, valve and nozzle v59, 6
  • a complete cycle of operation in accordance with the present invention may be divided into four primary periods-a blast period,; a make gas period, a reverse blast period and a reverse make period with purges between the primary periods.
  • stack valve H is closed, stack valve 451s, open and reversin valve it is set against No. 1 set.
  • Primary air is admitted through lines l5, l6,
  • valve ll, line I3 into the top of riser pipe 9 passcarrier gas employed as the propelling medium
  • the quantity of make gas produced may be so small as to make it difficult to recycle make gas at the initialstag'e of the make period and therefore the return of make gas may desirably'be dew layed for, by way of illustration, the first 30. sec-- onds.
  • an operator may wish to limit the degradation of make gas normally accomplished by recycling in which.
  • conduit 8 thereby partially preheating the air by its contact with the refractory lining before entering the bottom of chamber 5.
  • the partially preheated air passes upwardly through checkerbrick 6 thereby becoming heated to a higher temperature by refractory 8 and also burns any slightamount of carbon whichmay be deposited thereon.
  • the highly preheated air flows through orifice i into empty chambers wherein secondary air enters by way of lines 34, 32 and valve 33.
  • Heat oil pumped through lines 25, 2'5 and valve 28 discharges through, nozzle into the atmosphere of air whereupon the oil ignites, generating heat which is imparted to the walls of chamber 4. The quantity of.
  • air supplied should desirably be greater than that required for complete combustion of the heat oil, thereby pro viding an excess of air for burning any carbonaceous depositsfrom'the walls of chamber 4 made during a previousmake period.
  • Com bustion gases together with highly heated. secondary air pass'through crossover 35 downwardly throughempty chamber 38 heating its Walls and burning carbon thereon.
  • carbonaceous deposits unconverted into blue gas during the make period are utilized for heating the reaction chambers, efiecting a saving in heat oil consumed and in some instances eliminating the need for heat oil.v
  • the resultant combustion gases pass through orifice.
  • Alinear velocity of the mixture of steam and gas of about 50' feet per second will for most conditions of operation be found satisfactory.
  • vaporization of the oil occurs almost instantaneously in the empty space of reaction chamber 4 and substantially all the carbon liberated as a result of the vaporization and cracking of the oil therein will adhere to the internal surface of empty chamher 4.
  • this carbon Upon reaching incandescence this carbon will react with the steam to form blue gas. Carbon remaining on the walls ofchamber 4 will be converted to heat on a subsequent blast run.
  • the mixture of gases discharges from the top of chamber 4, through crossover 34 into empty chamber 38, also at a high temperature due to the previous blasting operation; wherein decomposition of the oil vapor molecules continues with further deposition of carbon on the walls of empty chamber 38 (minor in amountin com parison with the carbon deposited in chamber 4) and further production of bluefgas during the downward passage of the gas and steam'in vessel 35.
  • the gases are fixed by their downward passage through checkerbrick 4
  • may be accomplished in various manners, as for example by the use of a steam injector to withdraw a portion of the make gas from' the bottomof vessel 35 was an alternative to install a gas exhauster to withdraw make gas from the foul main and introducethe make gas with steam at the top of riserpipe [8. In some instances the'return of a portion of make gas from crossover 34 to riser pipe 9; or' the bottom of fixing chamber-1 may be fou'nd advantageous. It is not essential to admix the hydrocarbon carrier gas with the steam prior to passage through refractories 6 and therefore the carrier gas maybe commingled with the steam near the bottom. entrance of reaction chamber 4.
  • a normally gaseous hydrocarbon such as methane; ethane, propane or. mixtures thereof may be employed as the hydrocarbon carrier gas from an external source.
  • the combination of hydrocarbon carrier gas and my method of blasting and making have the cumulative efiect of reducing the'amount of carbon deposited which permits the use of smaller quantities of steam which in turn results 'in a higher calorific gassince the greater theamount of steam the lower the B.'t. u. content of the gas.
  • the make gases leaving'the bottom of vessel 35 pass through conduit -44 up through riser pipe 43 and thence discharge through conduit 5
  • the time for individual blast and make periods will vary dependent upon the nature of the charging oil, operating conditions, and quality of gas desired. Blast and make DBIiOdSjOf from 3-19 minutes duration will ordinarily "be found satisfactory. High superatmospheric Orsubatmospheric pressures are unnecessary since the operation of my process may becarriecl out efficiently at substantially atmospheric pressure.
  • the system In order to avoid an explosion hazard, the systemshould be purged of combustible gas prior to the introduction of air in the succeeding blast period. Purging may be accomplished by passing steam 1n through line 41 and out through the top ofriserpipell. a it In the practice of my process .a wide variety of charging stocks ranging from LP. gas to heavy liquid hydrocarbon oils may betreated.
  • a particular advantage of the present invention resides in the provision of an apparatus and process for the conversiontif low grade. hydrocarbon oils such as heavy cracked residuums having a Conradson carbon number in excess of 10 into high gravity low B. t. In.
  • a process for theproduction'of combustible gases which comprises; (a) a blast period wherein air passes downwardly througha previously heated riser pipe thereby effecting partial heat; ing of the air, upwardlythrough the'interstices of heated refractories contained in a first zone thereby further heating the air, passing the preheated air into asecond empty zone wherein secondary air and heat oil are introduced, which latter burns to impart heat to the'walls' of the empty zone, passing the combustion gases resulting from the reaction of the heat oil and air together with excess air downwardly through a third empty zone thereby transferring heat from the combustion gases to its walls and burning any carbonaceous deposits thereon by means.
  • a r v rse blast icdes csqri td in a b ve f a reverse urse DQ13051- dc..- r d n. there (92h er is period as de cr bed in ab and h).
  • a: rer rse p ee p r oda descr be. .d.- a g e 3- Ap a tu ap ed. for .cgn rt ie.
  • each vessel constructed to provide an empty chamber'above another chamher at least partially filled with refractory material with voids therebetween to permit passage of gas therethrough and'divided therefrom by a refractory orifice, two vertical refractory lined riser pipes extending upwardly to a height above the vessels with each riser pipe connected to the base of each vessel, a stack valve fitted to the top of each riser pipe, conduits leading from the top of each riser pipe connected to a threeway valve for reversal of fiow in the apparatus and for release of make gas, inlets for the introduction of primary air and steam into each riser pipe, conduits for the return of recycle make gas
  • a process for the production of combustible gas which comprises passing air upwardly through the interstices of heated refractories contained in a first zone thereby preheating the air, passing the preheated air into a'second empty zone wherein heating fluid is introduced, which latter burns to impart heat to the walls of the empty zone," passing the resultant combustion gases downwardly through a third empty zone thereby transferring heat from the combustion gases to its walls, continuing the passage of combustion gases downwardly through the interstices of refractories contained in a fourth zone thereby heating the refractories therein, and then discharging the combustion gases from the fourth zone; passing steam upwardly through the refractories of the first zone thereby heating and expanding the steam, passing the expanded steam upwardly into the second empty zonecountercurrent to downwardly injected hydrocarbon charging stock, maintaining the velocity of the steam, sufficiently high to substantially prevent passage .of carbonaceous material downwardly out of the second zone, withdrawing gaseous constituents substantially free of solid and liquid carbonaceous material from the top of the second empty

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US113765A 1949-09-02 1949-09-02 Manufacture of combustible gas Expired - Lifetime US2605176A (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
BE497277D BE497277A (enrdf_load_stackoverflow) 1949-09-02
US113765A US2605176A (en) 1949-09-02 1949-09-02 Manufacture of combustible gas
GB16000/50A GB683564A (en) 1949-09-02 1950-06-27 Manufacture of combustible gas
FR1022014D FR1022014A (fr) 1949-09-02 1950-07-13 Procédé et appareillage pour la fabrication de gaz combustible
DEA3069A DE847945C (de) 1949-09-02 1950-07-26 Verfahren und Einrichtung zur Erzeugung von brennbarem Gas aus Kohlenwasserstoffoel

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US683564XA 1949-09-02 1949-09-02
US1022014XA 1949-09-02 1949-09-02
US113765A US2605176A (en) 1949-09-02 1949-09-02 Manufacture of combustible gas

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US2605176A true US2605176A (en) 1952-07-29

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US113765A Expired - Lifetime US2605176A (en) 1949-09-02 1949-09-02 Manufacture of combustible gas

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US (1) US2605176A (enrdf_load_stackoverflow)
BE (1) BE497277A (enrdf_load_stackoverflow)
DE (1) DE847945C (enrdf_load_stackoverflow)
FR (1) FR1022014A (enrdf_load_stackoverflow)

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2700601A (en) * 1951-07-25 1955-01-25 Allied Chem & Dye Corp Process for producing a natural gas substitute from gas oil
US2700602A (en) * 1951-07-25 1955-01-25 Allied Chem & Dye Corp Process for producing a natural gas substitute from hydrocarbon oil
US2707675A (en) * 1952-02-11 1955-05-03 Inst Gas Technology Method of preparing fuel gas interchangeable with natural gas
US2714058A (en) * 1949-10-03 1955-07-26 Gas Machinery Co Method and apparatus for making oil gas
US2721123A (en) * 1952-05-10 1955-10-18 Inst Gas Technology Method of making oil gas interchangeable with natural gas
US2721122A (en) * 1952-09-24 1955-10-18 Inst Gas Technology Thermal method of making oil gas
US2734809A (en) * 1956-02-14 Method of making a fuel gas interchangeable with natural gas
US2734810A (en) * 1956-02-14 Method of making oil gas interchangeable with natural gas
US2734811A (en) * 1956-02-14 Method for the production of fuel gas from liquid fuels
US2739878A (en) * 1951-10-23 1956-03-27 Cons Water Power & Paper Co Vertically extending burner apparatus of the cyclone type
US2746850A (en) * 1953-09-24 1956-05-22 Gas Machinery Co Oil gas process and apparatus
US2755134A (en) * 1955-06-28 1956-07-17 Allied Chem & Dye Corp Atomizing spray for oil gas production
US2759806A (en) * 1953-02-16 1956-08-21 Inst Gas Technology Method of making a fuel gas
US2807528A (en) * 1954-04-19 1957-09-24 Inst Gas Technology Apparatus and cyclic regenerative process for making oil gas
US2829034A (en) * 1954-01-14 1958-04-01 Power Gas Ltd Manufacture of combustible gases
US2860959A (en) * 1954-06-14 1958-11-18 Inst Gas Technology Pressure hydrogasification of natural gas liquids and petroleum distillates
US2882138A (en) * 1957-05-27 1959-04-14 Inst Gas Technology Cyclic regenerative process for making fuel gas
US2907647A (en) * 1957-03-11 1959-10-06 Inst Gas Technology Cyclic regenerative process for catalytic gasification of petroleum
US2921845A (en) * 1956-01-23 1960-01-19 Gas Machinery Co Catalytic reforming of hydrocarbons
US2923609A (en) * 1956-10-22 1960-02-02 Humphreys & Glasgow Ltd Gas-making process
US2926077A (en) * 1955-05-02 1960-02-23 Totzek Friedrich Process of thermally cracking liquid hydrocarbons
US2927847A (en) * 1956-03-02 1960-03-08 Gas Council Heating gases and vapours
US2944806A (en) * 1956-01-23 1960-07-12 Power Gas Ltd Heating gases and vapours
US4131435A (en) * 1975-07-09 1978-12-26 Wilputte Corporation Automatic control apparatus for oil gas machine operation

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DE1075565B (de) * 1960-02-18 The Power Gas Corporation Limited, Stockton-on-Tees, Durham (Großbritannien) Verfahren und Vorrichtung zum Erhitzen von Gasen und/oder Dämpfen auf hohe Temperatur
DE1096880B (de) * 1953-03-13 1961-01-12 Didier Werke Ag Verfahren zur thermischen Herstellung von kohlenwasserstofffreien Synthesegasen aus gasfoermigen oder fluessigen Kohlenwasserstoffen
DE1036824B (de) * 1957-04-17 1958-08-21 Union Rheinische Braunkohlen Verfahren zur Herstellung von Wasserstoff und Kohlenoxyd durch Spalten von unter Normalbedingungen gasfoermigen Kohlenwasserstoffen mit Wasserdampf oder Kohlendioxyd an Nickelkatalysatoren

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US1821333A (en) * 1927-01-03 1931-09-01 Petroleum Conversion Corp Method of and apparatus for heating and mingling fluids
US2131696A (en) * 1935-12-16 1938-09-27 Combustion Utilities Corp Gas making apparatus
US2206189A (en) * 1937-07-19 1940-07-02 Sylvia Remsen Hillhouse Method of producing a fixed gas
US2174196A (en) * 1937-12-06 1939-09-26 Solvay Process Co Process for the manufacture of ethylene
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Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2734809A (en) * 1956-02-14 Method of making a fuel gas interchangeable with natural gas
US2734810A (en) * 1956-02-14 Method of making oil gas interchangeable with natural gas
US2734811A (en) * 1956-02-14 Method for the production of fuel gas from liquid fuels
US2714058A (en) * 1949-10-03 1955-07-26 Gas Machinery Co Method and apparatus for making oil gas
US2700601A (en) * 1951-07-25 1955-01-25 Allied Chem & Dye Corp Process for producing a natural gas substitute from gas oil
US2700602A (en) * 1951-07-25 1955-01-25 Allied Chem & Dye Corp Process for producing a natural gas substitute from hydrocarbon oil
US2739878A (en) * 1951-10-23 1956-03-27 Cons Water Power & Paper Co Vertically extending burner apparatus of the cyclone type
US2707675A (en) * 1952-02-11 1955-05-03 Inst Gas Technology Method of preparing fuel gas interchangeable with natural gas
US2721123A (en) * 1952-05-10 1955-10-18 Inst Gas Technology Method of making oil gas interchangeable with natural gas
US2721122A (en) * 1952-09-24 1955-10-18 Inst Gas Technology Thermal method of making oil gas
US2759806A (en) * 1953-02-16 1956-08-21 Inst Gas Technology Method of making a fuel gas
US2746850A (en) * 1953-09-24 1956-05-22 Gas Machinery Co Oil gas process and apparatus
US2829034A (en) * 1954-01-14 1958-04-01 Power Gas Ltd Manufacture of combustible gases
US2807528A (en) * 1954-04-19 1957-09-24 Inst Gas Technology Apparatus and cyclic regenerative process for making oil gas
US2860959A (en) * 1954-06-14 1958-11-18 Inst Gas Technology Pressure hydrogasification of natural gas liquids and petroleum distillates
US2926077A (en) * 1955-05-02 1960-02-23 Totzek Friedrich Process of thermally cracking liquid hydrocarbons
US2755134A (en) * 1955-06-28 1956-07-17 Allied Chem & Dye Corp Atomizing spray for oil gas production
US2921845A (en) * 1956-01-23 1960-01-19 Gas Machinery Co Catalytic reforming of hydrocarbons
US2944806A (en) * 1956-01-23 1960-07-12 Power Gas Ltd Heating gases and vapours
US2927847A (en) * 1956-03-02 1960-03-08 Gas Council Heating gases and vapours
US2923609A (en) * 1956-10-22 1960-02-02 Humphreys & Glasgow Ltd Gas-making process
US2907647A (en) * 1957-03-11 1959-10-06 Inst Gas Technology Cyclic regenerative process for catalytic gasification of petroleum
US2882138A (en) * 1957-05-27 1959-04-14 Inst Gas Technology Cyclic regenerative process for making fuel gas
US4131435A (en) * 1975-07-09 1978-12-26 Wilputte Corporation Automatic control apparatus for oil gas machine operation

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BE497277A (enrdf_load_stackoverflow) 1900-01-01
FR1022014A (fr) 1953-02-26
DE847945C (de) 1952-08-28

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