US3917468A - Synthetic natural gas production - Google Patents

Synthetic natural gas production Download PDF

Info

Publication number
US3917468A
US3917468A US422051A US42205173A US3917468A US 3917468 A US3917468 A US 3917468A US 422051 A US422051 A US 422051A US 42205173 A US42205173 A US 42205173A US 3917468 A US3917468 A US 3917468A
Authority
US
United States
Prior art keywords
carburant
zone
carburetting
gas
hot gas
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
Application number
US422051A
Other languages
English (en)
Inventor
Den Berg Godfried J Van
Frank K G Ouwerschuur
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell USA Inc
Original Assignee
Shell Oil Co
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Shell Oil Co filed Critical Shell Oil Co
Application granted granted Critical
Publication of US3917468A publication Critical patent/US3917468A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • C10J1/00—Production of fuel gases by carburetting air or other gases without pyrolysis
    • C10J1/213—Carburetting by pyrolysis of solid carbonaceous material in a carburettor
    • 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
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • 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
    • C01B3/36—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 using oxygen or mixtures containing oxygen as 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/26—Fuel 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

  • ABSTRACT A process for the production of synthetic natural gas or town gas is described wherein the hot gaseous product of the partial combustion of a carbonaceous fuel, containing hydrogen and carbon monoxide, is passed into a carburetting zone at a temperature of from 700 to ll00C and therein enriched with a volatile hydrocarbon content which on evaporation into the hot gaseous product of partial combustion is thermally cracked into methane and lighter unsaturated hydrocarbons.
  • the carburetted gas product is then passed into a hydrogenation zone maintained at a temperature sufficient to further decompose any remaining hydrocarbon wax and to lhydrogenate the unsaturated hydrocarbons.
  • a hydrogenation zone maintained at a temperature sufficient to further decompose any remaining hydrocarbon wax and to lhydrogenate the unsaturated hydrocarbons.
  • coke formation in the carburetting zone is substantially minimized by introducing the volatile hydrocarbon wax into the carburetting zone .in the form. of a thin layer of liquid which is maintained at a temperature below that at which thermalcracking occurs during the time the wax is not adsorbed by the hot gas stream.
  • This invention relates to an improved process for production of a synthetic natural gas of sufficient calorific value to be of use as town gas. More particularly, this invention is directed to a process wherein the gaseous product of partial combustion, being composed mainly of hydrogen and carbon monoxide which have relatively low calorific value, is upgraded in fuel value by mixing (carburetting) said gaseous product with the vapors of a volatile hydrocarbon at a temperature sufficient to thermally crack the hydrocarbon into methane and light unsaturated hydrocarbons, which are subsequently hydrogenated to afford a high-fuel value town gas, while at the same time avoiding problems tocoke formation which are inherent in such a carburetting procedure.
  • the gas thus produced has a relatively low calorific value, this being usually in the range of 1000 to 3000 kcal./Nm In order to be used as town gas, however, a calorific value of more than 5000 kcal./Nm is generally required.
  • the required increase in calorific value can be effected by combining the gas product of partial combustion, maintained at a temperature between 700 and 1 100C, with a stream of lighter weight volatile hydrocarbons which evaporate into the gas stream and are subsequently pyrolyzed.
  • the hot carburetted gas leaving the hydrogenator is cooled, for example to a temperature at which the soot and any hydrogen sulfide may be removed from it or at which a catalytic conversion of the carbon monoxide or a catalytic methane treatment can be carried out, and then desirably is further cooled in a waste heat boiler, since the amount of available heat is considerable and may be applied for the production of high pressure steam.
  • a waste heat boiler in which the hot gas is passed through helically-wound tubes which are externally 2 cooled by means of boiling water. The soot deposits less readily on the walls of the helical tubes than it does on the walls of straight tubes. The tubes therefore do not become choked with soot.
  • the present invention provides a solution for these and similar problems.
  • the instant invention provides a process for the production of synthetic natural gas or town gas which comprises a. partially combusting a carbonaceous fuel in a par tial combustion zone to produce a hot gaseous product containing hydrogen and carbon monoxide;
  • the process of the instant invention not only avoids the accumulation of coke or carbon deposits in the carburetting zone; but additionally does not require that the pressure of the alcohol be raised in advance of injection to a value well above the pressure of the gas in the carburetting zone in order to achieve high wax injection velocities.
  • another aspect of this invention is concerned with an apparatus for carburetting the hot gas product of the partial combustion of a carbonaceous fuel with a volatile hydrocarbon wax wherein the liquid alcohol is supplied to the carburetting zone as a thin layer or film which is maintained below cracking temperatures by externally supplied cooling on all those surfaces of the carburetting zone in which the alcohol is in contact before it is absorbed in the gas to be carburated.
  • FIG. 1 is a lateral view of an apparatus set up suitable for carrying out the process of the invention.
  • FIG. 2 is a partial cross-section of the carburetting apparatus according to the invention taken along line 2-2 of FIG. 1.
  • FIG. 3 is a diagrammatic drawing of an alternative embodiment of the carburetting apparatus according to the invention.
  • the invention relates to a process and apparatus for the production of a synthetic natural gas or town gas having a calorific value of more than 1,000 kcal. per Nm by partially combusting a carbonaceous fuel in a partial combustion zone comprising a refractory gasification reactor, carburetting the hot gas from the gasification reactor with a solvent at a temperature between 700C and 1 C in a carburetting zone which connects the gasification reactor to a hydrogenation zone, conducting the desired reactions in the carburetted gas in the hydrogenation zone (reactor) and cooling the gas obtained from the hydrogenation zone.
  • the first step of the process according to the invention involves a typical partial combustion procedure wherein a conventional carbonaceous fuel source, such as those detailed above (heavy fuel oil, coal grit, etc), is combined with less than the theoretical amount of oxygen present in an oxygen-containing gas at temperatures in excess of 1000C to yield a gaseous product containing as principal components, hydrogen and carbon monoxide. Since this step of the process is wholly conventional and quite well known by those skilled in the art it need not be detailed further herein.
  • a conventional carbonaceous fuel source such as those detailed above (heavy fuel oil, coal grit, etc)
  • the hot gas product of the partial combustion zone is then passed into the carburetting zone where it mixed with a volatile liquid hydrocarbon wax, the mixing occuring substantially in the vapor state.
  • the temperature of the hot gas throughout the carburetting zone ranges substantially between 700 and 1l0OC. This temperature is sufficient to cause the hydrocarbon content to thermally crack into methane and lower unsaturated hydrocarbon compounds on vaporization into the hot gas stream.
  • the rate at which the alcohol is introduced unto the carburetting zone for purposes of this invention can be conveniently expressed in terms of residence time in the car buretting zone, thus eliminating any dependence on specific carburetting zone size and shape.
  • the residence time of the liquid alcohol in the carburetting zone is preferably not less than 0.1 second or more than 1.0 second.
  • Carburetting is preferably carried out by passing liquid wax into the carburetting zone in a thin layer around a cooled rim along which flows the hot gas from the gasification reactor. As the hot gas flows along the rim the wax is absorbed by the gas and only becomes cooled at the very last moment. Since the wax passes around the rim it does not make earlier contact with the flowing gas, so that the temperature of the alcohol can easily be kept low.
  • the hot gas In order to achieve a gradual absorption of the wax by the hot gas, which, according to the invention, substantially prevents the formation of coke or carbon accumulations, it is preferred to pass the alcohol in the carburetting zone in a thin layer for some distance along a cooled wall alongwhich the said hot gas is flowing.
  • the said cooled wall suitably ends in a sharp transition, the liquid wax being partly absorbed by the said hot gas on its way along the cooled wall and the rest being absorbed at the sharp transition. Since care is taken that during the contact with the hot gas the velocity of the alcohol is not too high, no accumulation occurs.
  • the velocity of the flow of hot gas in the carburetting zone is preferably between and 1200 m/sec., the supply of alcohol being such that the thickness of the layer of alcohol film on the cooled wall is less than 1 mm.
  • the flow of the wax along the said cooled wall is preferably in the direction of flow of the hot gas.
  • the liquid solvent In order to keep the temperature of the liquid alcohol as low as possible, it is preferably supplied to the carburetting zone in a thin layer along a cooled wall along which the hot gas does not flow. The liquid alcohol is then suitably supplied along this cooled wall in a direction opposed to the direction of flow of the hot gas.
  • the invention is particularly suitable for a liquid wax consisting of a petroleum fraction, such as gas oil, naphtha and kerosine. It is especially these and similar waxs which tend to crack or polymerize on the injection nozzle in the conventional process.
  • the liquid solvent is supplied along a cooled wall along which there is no flow of hot gas, and then passed further along a cooled wall along which there is a flow of hot gas up to a sharp transition where the liquid alcohol is absorbed by the gas
  • a carburetting zone having a rotationally symmetrical or substantially rotationally symmetrical construction, thus minimizing the risk of accumulations in the carburetting zone.
  • the carburetted gas is passed into a hydrogenator in order to complete the desired reactions, i.e., to allow, inter alia, the evaporated wax to further decompose and unsaturated compounds to become hydrated.
  • the carburetted gas is very suitably passed into a hydrogenator where the gases are internally recirculated via an internal division of the hydrogenator.
  • An apparatus suitable for the production of gas having a calorific value of more than 1000 kcal. lNm comprises a refractory gasification reactor for the partial combustion of a fuel, a carburetting zone for carburetting the hot gas from the gasification reactor with a hydrocarbon wax, a hydrogenation reactor to conduct the desired reactions in the carburetted gas and optionally a waste heat boiler to cool the gas from the hydrogenator and produce steam.
  • this apparatus is characterized by means for 6 passing liquidoids in a thin layer into the carburetting zone and at the same time cooling the content.
  • the carburetting zone of the apparatus in general terms comprises a closed chamber, preferably cylindrical in shape, having (a) an inlet for introduction of the hot gas stream from the partial combustion zone whereby the flow of hot gas is directed along the axis of the closed chamber parallel to the walls of the closed chamber; (b) an inlet for introduction of the hydrocarbon curburant by which the alcohol enters the closed chamber at a direction perpendicular or opposed to the direction of the flow of hot gas and forms a thin film or layer on the surface of the closed chamber when .in contact with the hot gas; (c) a means for supplying external cooling, preferably by cooling devices in the chamber walls, to the surfaces of the closed chamber which are contacted by the thin layer of wax which is also in contact with the hot gas flow; and (d) an outlet for withdrawingthe carburetted hot gas mixture.
  • the carburetting zone of the above-mentioned apparatus preferably contains a rim with cooling devices wherein external cooling is supplied to the surface of the rim and means for passing the wax in liquid form around this rim, the rim being situated such that during operation the hot gas from the gasification reactor flows along it.
  • the carburetting zone suitalbly contains a wall with cooling devices to supply external cooling to the carburetting zone surface of the wall as well as means for passing the liquidoids along this wall, the wall being situated such that during operation the hot gas from the gasification reactor flows along it.
  • This wall with cooling devices preferably ends in a sharp transition.
  • the liquid wax is thereby gradually absorbed by the hot gas.
  • the carburetting zone preferably contains a wall with cooling devices and means for introducing the liquidoids into the carburetting zone along this wall, the wall [being situated such that during operation the hot gas does not flow along it. With such a carburetting zone there is no risk of accumulations occurring and the solvent can be supplied gradually.
  • the carburetting zone is preferably provided with a free wall with internal cooling devices which supply externally generated cooling to the wall surface, one side directed outwardly perpendicular to the axis of the closed chamber and one side facing the axis of the closed chamber.
  • internal cooling devices which supply externally generated cooling to the wall surface, one side directed outwardly perpendicular to the axis of the closed chamber and one side facing the axis of the closed chamber.
  • a functional apparatus is obtained when the carburetting zone has a rotationally symmetrical or substantially rotationally symmetrical construction.
  • a carburetting zone provided with a cooled .venturi-shaped contraction.
  • the solvent supply is mounted, so that an outer shell of the hot gas is pre-cooled in the first part of the venturi, before coming into contact with the cooled wax film in the second part.
  • the apparatus suitable for use in the process of the invention comprises an empty refractory gasification reactor 1, provided with a pipe 2 for the supply of fuel to the combustion chamber 3 of the 7 reactor and with a supply pipe 4 for the oxygen.
  • the apparatus also comprises a reactor discharge 5 arranged as a carburetting zone, this also being empty and being partly provided with refractory lining.
  • the carburetting zone comprises a hydrocarbon supply 6, through which liquid alcohol can be supplied to the jacket 7.
  • the discharge tube 5 is connected to a hydrogenator 9,10,11, consisting of two parallel columns 9 and 11, and a bent intermediate pipe 10.
  • This hydrogenator is empty and is entirely lined with refractory bricks.
  • the columns 9 and 11 are connected to the intermediate pipe by means of flanges l2 and 13, respectively.
  • the end of the upturned U- shaped hydrogenator is coupled to a waste heat boiler by means of a connection 14 and a flange 15.
  • This waste heat boiler consists of an empty-refractory brick-lined-bottom vessel 16 and a steam boiler 17 mounted vertically on the bottom vessel, which boiler is connected to the vessel 16 by means of a flange 18.
  • the steam boiler is equipped with a water supply 19 near its base and a discharge 20 for high-pressure steam at its top.
  • Through the stem boiler 17 runs a helically wound gas pipe 21, which communicates with the bottom vessel 16 via the straight bottom end 22 and which passes through the boiler wall at the top via the gas discharge 23.
  • FIG. 1 In carrying out the process according to the invention the apparatus shown in FIG. 1 operates as follows.
  • the fuel supplied via 2 together with less than the theoretical amount of oxygen is incompletely burned in reactor 1.
  • An amount of steam may optionally be supplied via the bumer or by other means.
  • a crude gas stream leaves the reactor via 5 at a temperature of approximately l200l400C.
  • This gas usually contains some soot and mainly comprises hydrogen and carbon monoxide. However, inter alia, water vapor, carbon dioxide, hydrogen sulfide are also usually present.
  • This hot crude gas is then carburetted in the discharge tube 5.
  • the gas should usually first be cooled below 1100C. It is also advantageous for an excess amount of water vapor to be present in the gas. To this end an amount of water is suitably injected into the tube 5 via 24 or into the bottom of the reactor via 25. A liquid wax in the form of a hydrocarbon fraction is then injected into the gas in one or more steps. If carburetting is carried out in several steps it is possible to inject additional water between two steps in order to cool the gas and to increaese the amount of water vapor present.
  • the crude carburetted gas which now contains a not inconsiderable percentage of methane, is passed into the bottom vessel of the waste heat boiler at a temperature between about 800C and 1100C, eventually leaving this waste heat boiler at a temperature of usually less than 400C.
  • the waste heat boiler produced steam under a considerable pressure.
  • the hydrogenator may be of an entirely different shape, and, for example, be arranged in a horizontal plane instead of vertically.
  • the waste heat boiler may also be different and, for example, have a number of helical gas pipes instead of one, have a differently shaped bottom vessel, or employ another coolant. It may also be of a completely different type.
  • FIG. 2 represents a horizontal partial cross-section of the carburetting apparatus taken along line 22 in FIG. 1.
  • the carburetting zone jacket 7 in FIG. 1 is not shown in FIG. 2.
  • this jacket surrounds the apparatus shown in partial cross-section including the discharge tube 5 which is shown.
  • a cylindrical inner wall 26 of the discharge tube 5 is provided with a refractory lining 33 of the carburetting zone in order to allow flow of the hot gas to be carburetted in flre direction indicated by the arrow.
  • the refractory lining 33 there is a ring groove 27 for the supply of liquidoids.
  • a cooled wall 28 with a cylindrically inverted inner part 29 projecting freely in the route of the flowing gas is arranged in the groove 27.
  • a Z-shaped profiled and cooled ring 30 is arranged under the ring (28,29) so as to form a Z-shaped slit 31.
  • the wax is introduced into the carburetting zone via this slit.
  • the side of the cooled wall (28,29) facing the ring 30 and the slit 31 faces the outside of the carburetting zone and the hot gas does not flow along it.
  • the side 32 of the cooled wall 29 freely mounted in the carburetting zone on the other hand is facing the center line of the carburetting zone; and the hot gases flow along it.
  • a suitable coolant is circulated through the passageways 50 and 51 to cool the walls 28,29 and 30 by conduit means coupled to the openings between the walls (not shown in FIG. 2).
  • the liquid wax is passed into the carburetting zone in a thin layer via the cooled slit 31, that is to say, via the rim 34 to the side 32 along which the hot gas is flowing.
  • the remaining liquid content can be absorbed by the hot gas.
  • Part of the liquid wax is already absorbed by the hot gas between the rims 34 and 35.
  • the carburetting zone may be constructed differently and possess, for example, differently shaped walls for the introduction of liquid alcohol.
  • FIG. 3 is a diagrammatic illustration of such an alternative carburetting zone.
  • the connecting tube 36 which connects the gasification reactor (not shown) with the hydrogenator 37, contains a carburetting zone.
  • This tube 36 has a cooled rotationally symmetrical restriction 38, 39, which is situated on either side of a ring slit 40 for the supply of liquidoids.
  • the hot gas to be carburetted flows into the carburetting zone via the jacket 7 and through the tube 36in the direction indicated by the arrow, and the wax is supplied to the ring slit 40 in the direction likewise indicated.
  • the liquidoids then enters the carburetting zone in a thin layer along the inner side 41 of the cooled wall 38along which the hot gas is also flowing.
  • the cooling of the walls of the striction 38 and 39 is diagrammatically illustrated by the water shells 42 and 43.
  • a particular advantage of this embodiment of the carburetting zone is that the part of the hot gas that comes into contact with the wax film on the wall 38 is cooled in advance on wall 39.
  • the gas After having been carburetted the gas enters the hydrogenator 37 via connecting tube 36, and is hydrogenated. The gas subsequently passes from the hydrogenator to a waste heat boiler (not shown) to be cooled.
  • a process for the production of town gas which comprises a. partially combusting a carbonaceous fuel selected from the class consisting of heavy fuel oil, petroleum distillates or residues, liquid fuel containing process soot and slurries of coal grit in water in a partial combustion zone to produce a hot gaseous product containing hydrogen and carbon monoxide;

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Industrial Gases (AREA)
  • Solid-Phase Diffusion Into Metallic Material Surfaces (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
US422051A 1972-12-15 1973-12-05 Synthetic natural gas production Expired - Lifetime US3917468A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
NLAANVRAGE7217059,A NL171597C (nl) 1972-12-15 1972-12-15 Werkwijze en inrichting voor de bereiding van gas door partiele verbranding gevolgd door carbureren.

Publications (1)

Publication Number Publication Date
US3917468A true US3917468A (en) 1975-11-04

Family

ID=19817552

Family Applications (1)

Application Number Title Priority Date Filing Date
US422051A Expired - Lifetime US3917468A (en) 1972-12-15 1973-12-05 Synthetic natural gas production

Country Status (13)

Country Link
US (1) US3917468A (de)
JP (1) JPS5748597B2 (de)
BE (1) BE808277A (de)
CA (1) CA1014741A (de)
DD (1) DD108720A5 (de)
DE (1) DE2362032C2 (de)
ES (1) ES421419A1 (de)
FR (1) FR2327306A1 (de)
GB (1) GB1451937A (de)
IN (1) IN138705B (de)
IT (1) IT1000835B (de)
NL (1) NL171597C (de)
ZA (1) ZA739450B (de)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS52142702A (en) * 1976-05-24 1977-11-28 Agency Of Ind Science & Technol Gasification of a mixture of coal and heavy oil
US4078989A (en) * 1976-05-11 1978-03-14 Leas Brothers Development Corporation Coal conversion process
WO2003066517A1 (en) * 2002-02-05 2003-08-14 The Regents Of The University Of California Production of synthetic transportation fuels from carbonaceous materials using self-sustained hydro-gasification
US20070293713A1 (en) * 2002-11-13 2007-12-20 Regents Of The University Of Minnesota Catalytic partial oxidation of hydrocarbons
US20080021121A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US20080021122A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Operation of a steam methane reformer by direct feeding of steam rich producer gas from steam hydro-gasification
US20080312348A1 (en) * 2006-07-18 2008-12-18 Chan Seung Park Method and apparatus for steam hydro-gasification with increased conversion times
US20090094892A1 (en) * 2006-07-18 2009-04-16 Norbeck Joseph M Commingled coal and biomass slurries
US20090221721A1 (en) * 2002-02-05 2009-09-03 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US8349288B2 (en) 2006-12-06 2013-01-08 The Regents Of The University Of California Process for enhancing the operability of hot gas cleanup for the production of synthesis gas from steam-hydrogasification producer gas

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2716597A (en) * 1951-06-12 1955-08-30 Koppers Co Inc Method and apparatus for the production of combustible gases from liquid fuels
US2971829A (en) * 1958-12-23 1961-02-14 Shell Oil Co Hydrocarbon gasification

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US992944A (en) * 1905-06-29 1911-05-23 Henry L Doherty Method of enriching gas for illuminating purposes.
DE839400C (de) * 1950-12-20 1952-05-19 Carl Miedbrodt Verfahren zur Erzeugung von oelkarburiertem Wassergas

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2716597A (en) * 1951-06-12 1955-08-30 Koppers Co Inc Method and apparatus for the production of combustible gases from liquid fuels
US2971829A (en) * 1958-12-23 1961-02-14 Shell Oil Co Hydrocarbon gasification

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4078989A (en) * 1976-05-11 1978-03-14 Leas Brothers Development Corporation Coal conversion process
JPS5441606B2 (de) * 1976-05-24 1979-12-10
JPS52142702A (en) * 1976-05-24 1977-11-28 Agency Of Ind Science & Technol Gasification of a mixture of coal and heavy oil
WO2003066517A1 (en) * 2002-02-05 2003-08-14 The Regents Of The University Of California Production of synthetic transportation fuels from carbonaceous materials using self-sustained hydro-gasification
US8603430B2 (en) 2002-02-05 2013-12-10 The Regents Of The University Of California Controlling the synthesis gas composition of a steam methane reformer
CN1642851B (zh) * 2002-02-05 2010-04-14 加利福尼亚大学董事会 采用自支持加氢气化从含碳材料制备合成运输燃料
US20090221721A1 (en) * 2002-02-05 2009-09-03 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US7534372B2 (en) * 2002-11-13 2009-05-19 Regents Of The University Of Minnesota Catalytic partial oxidation of hydrocarbons
US20070293713A1 (en) * 2002-11-13 2007-12-20 Regents Of The University Of Minnesota Catalytic partial oxidation of hydrocarbons
US20090094892A1 (en) * 2006-07-18 2009-04-16 Norbeck Joseph M Commingled coal and biomass slurries
US20080312348A1 (en) * 2006-07-18 2008-12-18 Chan Seung Park Method and apparatus for steam hydro-gasification with increased conversion times
US20080021122A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Operation of a steam methane reformer by direct feeding of steam rich producer gas from steam hydro-gasification
US7897649B2 (en) 2006-07-18 2011-03-01 The Regents Of The University Of California Operation of a steam methane reformer by direct feeding of steam rich producer gas from steam hydro-gasification
US8118894B2 (en) 2006-07-18 2012-02-21 The Regents Of The University Of California Commingled coal and biomass slurries
US8143319B2 (en) 2006-07-18 2012-03-27 The Regents Of The University Of California Method and apparatus for steam hydro-gasification with increased conversion times
US8268026B2 (en) 2006-07-18 2012-09-18 The Regents Of The University Of California Controlling the synthesis gas composition of a steam methane reformer
US20080021121A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US8349288B2 (en) 2006-12-06 2013-01-08 The Regents Of The University Of California Process for enhancing the operability of hot gas cleanup for the production of synthesis gas from steam-hydrogasification producer gas

Also Published As

Publication number Publication date
ZA739450B (en) 1974-11-27
BE808277A (nl) 1974-06-06
IT1000835B (it) 1976-04-10
DD108720A5 (de) 1974-10-05
NL171597B (nl) 1982-11-16
GB1451937A (en) 1976-10-06
DE2362032A1 (de) 1974-06-27
FR2327306B1 (de) 1978-04-21
NL7217059A (de) 1974-06-18
ES421419A1 (es) 1976-05-01
FR2327306A1 (fr) 1977-05-06
DE2362032C2 (de) 1982-10-07
JPS4989701A (de) 1974-08-27
CA1014741A (en) 1977-08-02
JPS5748597B2 (de) 1982-10-16
NL171597C (nl) 1983-04-18
IN138705B (de) 1976-03-20

Similar Documents

Publication Publication Date Title
US5261602A (en) Partial oxidation process and burner with porous tip
US4353712A (en) Start-up method for partial oxidation process
US4443228A (en) Partial oxidation burner
US4491456A (en) Partial oxidation process
EP0127273B1 (de) Brenner und Teilverbrennungsverfahren fester Brennstoffschlämme
US4113445A (en) Process for the partial oxidation of liquid hydrocarbonaceous fuels
EP0343735B1 (de) Verfahren zur Partielloxydation von flüssigen oder festen und/oder gasförmigen Kohlenwasserstoff enthaltendem Brennstoff
US4400179A (en) Partial oxidation high turndown apparatus
US3972690A (en) Gasification process
US4038186A (en) Carbon decanter
CN1136800A (zh) 富氢气体的生产
US4392869A (en) High turndown partial oxidation process
US4351647A (en) Partial oxidation process
US4014786A (en) Carbon separation
US3917468A (en) Synthetic natural gas production
US4351645A (en) Partial oxidation burner apparatus
US4007019A (en) Production of clean synthesis or fuel gas
US3816332A (en) Synthesis gas production
US4007018A (en) Production of clean synthesis or fuel gas
US4411670A (en) Production of synthesis gas from heavy hydrocarbon fuels containing high metal concentrations
US2346754A (en) Fuel oil gasification
US4371378A (en) Swirl burner for partial oxidation process
US4007017A (en) Production of clean synthesis or fuel gas
US4402709A (en) Simultaneous production of clean dewatered and clean saturated streams of synthesis gas
US3480416A (en) Gas preparation process and apparatus