US2976134A - Hydrocarbon conversion process - Google Patents

Hydrocarbon conversion process Download PDF

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US2976134A
US2976134A US626909A US62690956A US2976134A US 2976134 A US2976134 A US 2976134A US 626909 A US626909 A US 626909A US 62690956 A US62690956 A US 62690956A US 2976134 A US2976134 A US 2976134A
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dispersion
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Peter L Paull
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Texaco Development Corp
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    • 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
    • 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
    • C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
    • C01B3/28—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles
    • C01B3/30—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using moving solid particles using the fluidised bed technique
    • 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
    • C01B3/38—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 catalysts
    • C01B3/388—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 catalysts the heat being generated by superheated steam
    • 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

Definitions

  • This invention relates to a'method and apparatus vfor the conversion of carbonaceous. fuels togases
  • 'it is ⁇ directed to a Iprocess-for the continuous and complete conversion of ⁇ heavyoils into fixed gases of high calorific value.
  • 'By heavy oil is meant'an oil which cannot be completely vaporized :by heat ⁇ alone without cracking and the formation of'carbonaceous deposits under gasification pressure, for ⁇ example, crude oil, reduced crude, cracking plant residual oil Vand coal tar.
  • thejinvention relates tothe lconversion of heavy oilsto high ⁇ B.t; ⁇ u. gases bythe following steps: A ydispersion of heavy oil in steam Vis klformed by subjectinga vmixture of heavy oil vandsteam to highly turbulent fio'w conditionsin va preheater. ⁇ A synthesis gas comprising carbon monoxideand hydrogen yis generated at elevated temperaturefand pressure ⁇ bythe Vpartial combustion of a'carbonaceous Yfuel withoxyg'en.
  • the preheated steam-heavy'oil dispersion and hotV syn- Vthesis-gas are combined' and the combinedstream'is contacted -with a cracking catalyst to 'effect cracking and generation of a gas of high B tu. content.
  • the resultant product gas is suitable for distribution'as fuel.
  • the usual method -of kmanufacturing gas from heavy oils is to spray rvthe heavy-oil into 1a furnace containing a checkerwork of heated brick or other refractory material.
  • the oil is thus subjected to severe cracking which converts the oil to gaseous products, which are withdrawn from the furnace, and a carbonaceous residue which deposits up'o'n the checkerwork.
  • the - ⁇ furnaces areheated by burning oil or gas .therein and by burningthe car- 'bonaceous residue from the checkerwork "byi blasting the furnace with air. This process necessarily-employs alterrnatingheating and cracking cycles.
  • the'heavy oil feed is injected into a stream of steam and the/resulting mixture subjected to .highly turbulent flow conditions.
  • the mixture is passed into an elongated tubular f m l l 2,976,134 ce Patented Mar. 21, 19761 2 av substantially homogeneous dispersion having the appearance of a mist.
  • the steam is superheated prior to injection of the oil to a temperature such that there is substantially no'condensation of the steam in the resulting steam oil mixture.
  • the oil may be preheated to a temperature up to about 700 F. or may be at ambient temperature when injected into the stream of preheated steam.
  • the dispersion is preferably formed by passing the oil-steam mixture through a relatively Ylong tubular conduit at a velocity in excess of about 20 feet per second, preferably in excess of 50 feet persecond. Lower velocities permit partial segregation Vof the oil, -probably along the walls of theconduit, resultingin uneven flow of the dispersion,
  • the tubular'section in which the dispersion of oil 'in steam is accomplished vhas a length at least 100 times the inside pipe diameter.
  • the mixing tube' has a length -at least V500 times its inside diameter.
  • Toravoid slugging-and tto insure a-uniform dispersion, -suflicient vapor, i.e.,fstearn-and Vapor ⁇ from the oil, must be'present so that-atleast 70 percent by volume of the vfee'd -is in-vapor form.
  • the tubular mixing zone is heated to a ternperature above the temperature of the initial mixture of :steam and oil ⁇ so that-the mixture is preheated during "flow therethrough. n
  • the lrelative proportions of steam and yoil may vary -over a-widevrange, -forexample, ⁇ from about0.2 to about ⁇ 3 pounds Aoffs'tearnper pound of oil supplied to the -reaction zone.
  • A'preheated dispersion Vof oil in steam prepared -in 'the manner-described above is admixed with .the etituent from a partial combustion zone.
  • the partial combustion 5:1.fon'e for example, ismaintained at a temperature 'with- 'inth'e range of about i800 to 3500 F. at a level where 4the kreaction goes rapidly to completion.
  • the products of combustion comprise carbon monoxide and hydrogen substantially lfree -from methane.
  • the lower temperatures for example, 'in the tangent-1800 to 2200io F.
  • the catalyst may be disposed as a fixed bed or may be in the form of pulverulent solids. Although substantially less Acarbon ⁇ is formediin the process of this invention than'is'formed .in other processes for the gasification of heavy' oils, some carbonaceous deposits form on the catalyst. These deposits may be readily removed from fixed bedsl ofcatavlyst by discontinuing processing, and burning off thecarlbonaceous deposits with oxygen or oxygen-containingA gas streams, for example, air orair diluted vwith lineages. When a fluidized solids catalyst is used, the catalyst may be readily ⁇ separated from the product gases and a portion continuously regenerated by passing to a uidized bed regenerator where the carbonaceous deposits are burned with a stream of air.
  • Pressure in itself is not critical in the dispersion step.
  • the temperature and pressure relationships relating to vaporization are well known. Steam and oil are passed through the dispersion coil at a pressure such that the steam-oil dispersion is discharged at a pressure at least as high as the subsequent gasification zones. A considerable pressure drop takes place in the dispersion coil due to resistance to ow which may be, for example, about 100 pounds per square inch.
  • gas generation zone and cracking zone In the generation of fuel gas it is desirable to operate the gas generation zone and cracking zone at a superatmospheric pressure, preferably within the range of about 150 to about 1500 pounds per square inch gage.
  • a superatmospheric pressure preferably within the range of about 150 to about 1500 pounds per square inch gage.
  • Carbonaceous fuels generally may be employed in the partial combustion step of the process of this invention.
  • pulverized coal may be gasied by partial combustion with oxygen to provide a stream of carbon monoxide and hydrogen at temperatures in the range of about 1800 to 3500 F.
  • the heavy oil dispersion prepared as described above is employed in the cracking step of the process of this invention.
  • An advantage of the process of this invention is that the tendency of heavy hydrocarbon oils to form carbonaceous deposits on the catalyst when employing these oils for catalytic gasification is substantially reduced.
  • the uniform dispersion of oil in steam employed in this process avoids the formation of carbonaceous deposits caused by overcracking which occurs as a result of irregular wetting of catalyst by droplets of oil.
  • the tendency of oil to form carbonaceous deposits during heating is avoided by my method of heating the oil dispersion since only a part of the heating is effected in tubular heaters and the nal increase to cracking temperature is effected by injecting the dispersion into hot synthesis gas. Further, conducting ⁇ the cracking reaction in the presence of a gas comprising carbon monoxide and hydrogen tends to suppress the formation of carbonaceous deposits.
  • steam-oil dispersions may be readily formed at superatmospheric pressures, for example about 100 to 1500 pounds per square inch. Dispersions formed in accordance with the method of this process permit the uniform distribution of charge components throughout a catalytic reactor equvalent to the distribution of completely vaporized charge oils. Accordingly this method provides an improved means to charge a heavy oil to a catalytic reactor under pressures at which the heavy oil could not be vaporized without cracking.
  • Figure I illustrates a form of the process of this invention in which a dispersion of a heavy oil in steam is formed, a part of said dispersion is subjected to partial combustion and another part of said dispersion is admixed with the products of partial combustion and the combined stream contacted with cracking catalyst at cracking temperatures to produce a gas of high calorific value.
  • Water is introduced into the system by pump which feeds water to heating coil 11 in heater 12 where the water is converted to steam.
  • the steam produced in coil 11 is discharged through line 13.
  • Heavy oil from an external source not shown is pumped at a controlled rate by pump 15 through line 16 and is combined with the stream from line 13 inline 17.
  • Pumps 10 and 15 for water and oil respectively permit accurate proportioning of the steam and oil.
  • the mixture of oil and steam which is at iirst rather crude, is developed into an intimate dispersion af oil particles in steam by passage through a long tubular zone at relatively high velocity, preferably in excess of 50 feet per second, so that the highly turbulent ow thoroughly and evenly disperses the oil droplets in the steam.
  • the steam-oil mixture passes through heating coil 18 in heater 19.
  • the oil is continuously injected into the stream of steam in desired proportions and subjected in heating coil 18 to a ternperature within the range of about 300 to l000 F.
  • a part of the resulting steam-oil dispersion passes through lines 21 and 22, ilow control valve 23 and line 24 to burner 26 where it is mixed with oxygen from line 27 and discharged directly into gas generator 2S.
  • Oxygen is introduced through line 27 into burner 26 at a rate controlled by regulator 29.
  • a suitable burner for the partial combustion of oil with oxygen is described in the copending application of Leon P. Gaucher, Serial Number 266,840, tiled January 17, 1952, now Patent Number 2,810,433.
  • the generator 2S comprises a pressure vessel 30 provided with a suitable refractory and heat insulating lining 31 enclosing a compact, unpacked reaction chamber. Products of reaction ow through outlet 32 which cornmunicate with cracking reactor 33. Another part of the steam-oil dispersion in line 21 passes through line 34, regulator 36 and line 37 and is continuously injected into gas generator outlet 32.
  • the hot product gases leaving generator 28 at substantially the temperature of the generator, in the range of about 1800 to 3500 F., are continuously contacted with steam-oil dispersion from line 37 to form a combined stream at a temperature Within the range of about 1000 to l600 F. and the combined stream passes into cracking reactor 33.
  • Cracking reactor 33 comprises a pressure vessel 38 in which one or more beds of cracking catalyst 39 are disposed. Any of the well-known cracking catalysts may be used in the process of this invention. Iron group metal catalysts and bauxite, for example, are suitable; nickel catalysts or catalysts containing nickel and chromium are preferred. Cracking of the heavy oil and reaction of the synthesis gas in the combined stream to produce a high B.t.u. gas is effected at a temperature within the range of about 1000 to 1600" F. and at a pressure within the range of about to 1500 pounds per square inch. Products are withdrawn from reactor 33 as the product gas of this process and are dicsharged for distribution or use not shown.
  • Figure II illustrates a form of the process of this invention in which coal is gasiiied by partial combustion with oxygen to form a gas comprising carbon monoxide and hydrogen, a steam-oil dispersion is formed as described heretofore, the partial combustion products and steam-oil dispersion are admixed and the combined stream is cracked in the presence of a uidized solids catalyst to form heating gas of highskyic value.
  • Crushed coal from an externalsource notlshown is fed into ⁇ mixer '51 operated at atmospheric pressure wherein it is admixed with sufficient water from line 52 to form a iiuid slurry.
  • the slurry is passed through line 53 into a thickener V54. Excess water is eliminated from the slurry in thickener 54 andV recycled tothe mixer in line 56.
  • Resulting slurry containing only su'icient water to render it tiuid is -wi-thdrawn from thickener ⁇ 54 through line 57 and charged at elevated pressure by means of pump 58 through line 59 to heating coil 61 in heater 62.
  • the water is vaporized in the heater dispersng the powdered coal in steam.
  • the dispersion is passed through line 63 into separator 64 where excess steam is withdrawn for heating or other uses not shown through line 66 and regulator 67.
  • Steam-coal dispersion is withdrawn from separator 64 through line 68 and is discharged into generator 69 Ythrough a suitable burner 71.
  • Oxygen is admitted to -burner7 1 through line 72 to maintain the temperature in'thegenerator within the range of 2200 to 3500 F., preferably in the range of about 2200 to 2800 F.
  • Generator69 may comprise a steel shell 73 designed to withstand the internal operating pressure which may be within the range of about 100 to 1500 pounds per square inch.
  • the gas generator section islined with a suitable 'refractory 74 to withstand the high temperatures generated within the gas generation zone and to protect the shell from overheating.
  • a partition 76 divides the vessel into two separate zones, the gas generation zone 69 and a slag separator or slag pot 77.
  • Product gases from the gas generator pass into the slag pot where hot gases are separated and withdrawn through line 78 and the slag falls to the bottom of the slag pot and is quenched by water introduced through line 79. Solidied slag and water are withdrawn fordisposal through line 81.
  • Water is introduced through pump 79 and line 81 into heating coil 82 in heater 83 to generate steam.
  • Steam from heating coil 82 discharges through line 84.
  • Heavy oil from an external source not shown is pumped by pump 86 through line 87 and combined with the steam in line 84.
  • the mixture of steam and oil is passed through line 88 to heating coil 89 in heater 91.
  • the intimate dispersion of oil in steam formed by passage through heating coil 89 discharges through line 92 and is combined with the hot gases in line 78 to form a combined stream in line 93 at a temperature within the range of about 1000 to 1600 F.
  • the combined stream in line 93 is contacted with regenerated catalyst from line 94 and is passed through line 96 and inlet cone 97 to cracking reactor 98.
  • a uidized bed of bauxite cracking catalyst 99 is maintained in reactor 98.
  • the combined stream of oil-steam dispersion and partial combustion products is cracked in reactor 98 at 1400 F. and 300 pounds per square inch pressure to form high B.t.u. gas which passes through cyclone separator 1011 and outlet line 102 for external use not shown.
  • a carbonaceous deposit forms on the catalyst. This carbonaceous deposit is continuously removed by withdrawing a portion of the catalyst from cracking reactor 98 through sandpipe 103 and regulator 104 for regeneration.
  • Air from compressor 106 is discharged through line 107 to entrain catalyst from standpipe 103 and transfer it to regeneraftor 10S through transfer line 109 and regenerator inlet cone 111.
  • a uidized bed of catalyst 112 is maintained in regenerator 108 and the carbonaceous deposit on the catalyst is lremoved by combustion. Flue gas passes through cyclone separator 113 and is discharged through line 114 to the atmosphere. Regenerated catalyst is withdrawn from regenerator 108 through standpipe 94 and regulator 116 for recycle to the cracking reactor.
  • Example A reduced crude yoil characterized by a gravity of 14.4 API, a furol viscosity of 200 seconds at ⁇ 122 F., an ash content of 0.1 weight percent and an ultimate analysis of 85.1 weight percent carbon, 11.0 weight percent hydrogen and 3.9 weight percent sulfur is converted toa high B.t.u. fuel gas by the process of this invention.
  • Steam is generated at a Irate of 12,668 pounds per hour and is admixed with 25,852 pounds per hour of the aforesaid oil preheated to a temperature of 220 F.
  • the mixture at a pressure of 1000 pounds per square inch is passed through a heating coil at a velocity of 55 feet per second wherein the temperature is raised to 750 F.
  • Gas from the partial combustion zone at substantially the temperature of the partial combustion zone is admixed with 20,264 pounds per hour of the steam oil dispersion prepared above.
  • the resulting mixture at a temperature of l,580 F. ⁇ and at substantially the pressure of the partial combustion zone is passed through a xed bed of 15.9 cubic feet of a nickel cracking catalyst.-v Eight hundred sixty eight thousand cubic feet per hour of a fuel gas having a heating value of 575 B.t.u. per cubic foot (dry basis) are produced.
  • a process for the conversion of a heavy oil to fuel y gas of high calorilic value which comprises introducing a heavy oil into a stream of steam, subjecting ⁇ the resulting mixture of oil and steam to high turbulence effecting dispersion of said oil in steam while maintaining at least a portion of said oil in a liquid phase, introducing a part of said dispersion in admixture with oxygen into a partial combustion zone, effecting partial combustion of said oil to form a gas comprising carbon monoxide and hydrogen at a temperature within the range of about 1800 to 3500 F., admixing with said hot gas a part of said dispersion to form a combined stream at a temperature within the range of about 1000 to 1600 F., contacting said'combined stream at said temperature with a cracking catalyst, and recovering a composite gas of relatively high heating Value as a product of the process.
  • a process for the generation of a fuel gas of high caloric value which comprises subjecting a carbonaceous fuel to partial combustion to form a gas comprising carbon monoxide and hydrogen at a temperature within the range of about 1800 to 3500 F. and at a pressure within the range of about 100 to 1500 pounds per square inch, mixing said gas comprising carbon monoxide and hydrogen with a dispersion of heavy oil in steam to form a combined stream at a temperature Within the range of 1000 to 1600 IF., said dispersion of heavy oil in steam being formed by introducing a heavy oil into a stream of steam in proportion within the range of about 20 to 300 percent by weight of steam basis the weight of heavy oil and passing the resulting mixture of oil and steam at a velocity in excess of 20 feet per second through a tubular conduit having a length at least 100 times its inside diameter effecting dispersion of said oil in said steam while maintaining a portion of said oil in the liquid phase, contacting said combined stream with an iron group metal cracking catalyst at a temperature within the range of about 1000 to 1600 F., and

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Description

March 21, 1961 P. L. PAULL HYDROCARBON CONVERSION PROCESS 2 SheetsSheet 1 Filed Dec. 7, 1956 March 21, 1961 P. L. PAULI. 2,976,134
HYDROCARBON CONVERSION PROCESS Filed Dec. 7, 1956 2 Sheets-Sheet 2 United States Patent C) HYDROCARBON CONVERSIN PROCESS Peter L. Paull, Westport, Conn.,"assignor 'to Texaco Development Corporation, New York, N.Y., a corporation of Delaware Filed Dec. 7, 1956, Ser. No. 626,909
11 Claims. `(Cl. 48-'215) This invention relates to a'method and apparatus vfor the conversion of carbonaceous. fuels togases In onei of 'its more specific aspects, 'it is `directed to a Iprocess-for the continuous and complete conversion of `heavyoils into fixed gases of high calorific value. 'By heavy oil is meant'an oil which cannot be completely vaporized :by heat `alone without cracking and the formation of'carbonaceous deposits under gasification pressure, for `example, crude oil, reduced crude, cracking plant residual oil Vand coal tar. j
In a preferredembodiment, thejinvention relates tothe lconversion of heavy oilsto high `B.t;`u. gases bythe following steps: A ydispersion of heavy oil in steam Vis klformed by subjectinga vmixture of heavy oil vandsteam to highly turbulent fio'w conditionsin va preheater. `A synthesis gas comprising carbon monoxideand hydrogen yis generated at elevated temperaturefand pressure `bythe Vpartial combustion of a'carbonaceous Yfuel withoxyg'en.
'The preheated steam-heavy'oil dispersion and hotV syn- Vthesis-gas are combined' and the combinedstream'is contacted -with a cracking catalyst to 'effect cracking and generation of a gas of high B tu. content. The resultant product gas is suitable for distribution'as fuel.
The usual method -of kmanufacturing gas from heavy oils is to spray rvthe heavy-oil into 1a furnace containing a checkerwork of heated brick or other refractory material. The oil is thus subjected to severe cracking which converts the oil to gaseous products, which are withdrawn from the furnace, and a carbonaceous residue which deposits up'o'n the checkerwork. The -`furnaces areheated by burning oil or gas .therein and by burningthe car- 'bonaceous residue from the checkerwork "byi blasting the furnace with air. This process necessarily-employs alterrnatingheating and cracking cycles. It has not been-pos- -sible to crack heavy oils completely yto gas in tubular heaters since such lsevere cracking results in the formation of carbon and the plugging of heater tubes. Catalytic 'processeshave been developed for? reforming light hydrocarbons, .for example,methane, With steam to generate hydrogen andcarbon oxides but these processes have not been successfully employed with Sh'e'avier hydrocarbons, such as fuel oils, because of 'rapid catalystfouling by carbonaceous deposits.
I have now found that'the ltendency of heavy oils'to form carbonaceous deposits `in catalytic gasification reactions can be materially reduced by the Yprocess of my invention to make such catalytic gasification processes economical and practical. Inaccordance with'the proc- Aess of this invention, the'heavy oil feed is injected into a stream of steam and the/resulting mixture subjected to .highly turbulent flow conditions. In a preferred embodiment, the mixture is passed into an elongated tubular f m l l 2,976,134 ce Patented Mar. 21, 19761 2 av substantially homogeneous dispersion having the appearance of a mist.
Preferably, the steam is superheated prior to injection of the oil to a temperature such that there is substantially no'condensation of the steam in the resulting steam oil mixture. The oil may be preheated to a temperature up to about 700 F. or may be at ambient temperature when injected into the stream of preheated steam. The dispersion is preferably formed by passing the oil-steam mixture through a relatively Ylong tubular conduit at a velocity in excess of about 20 feet per second, preferably in excess of 50 feet persecond. Lower velocities permit partial segregation Vof the oil, -probably along the walls of theconduit, resultingin uneven flow of the dispersion,
and vpressure and 'flow rate fluctuations, or slugging, of
thefuelfeed tothe generator or gasification reactor. Prferably, the tubular'section in which the dispersion of oil 'in steam is accomplished vhas a length at least 100 times the inside pipe diameter. Advantageously, the mixing tube'has a length -at least V500 times its inside diameter. Toravoid slugging-and tto insure a-uniform dispersion, -suflicient vapor, i.e.,fstearn-and Vapor `from the oil, must be'present so that-atleast 70 percent by volume of the vfee'd -is in-vapor form. Preferably, at least 90 mol percent of the oil-steam feed'is yin'vapor form. In a preferred embodiment, the tubular mixing zone is heated to a ternperature above the temperature of the initial mixture of :steam and oil `so that-the mixture is preheated during "flow therethrough. n
`The lrelative proportions of steam and yoil may vary -over a-widevrange, -forexample,` from about0.2 to about `3 pounds Aoffs'tearnper pound of oil supplied to the -reaction zone. The'leffectiveness of the -degree "of disper- `sionof the oil `in fsteam -varies little with the `porportionsofsteam and-oil Within-the above range. `This :is of l#particular advantagefrom the'standpoint'thatlthe rate -f steamffed to the reaction zone may be regulatedexclusively'on the basis of the operating requirementsan"d particularly"the'temperature which it is desired to main- 'tain inthe reaction zone.
A'preheated dispersion Vof oil in steam prepared -in 'the manner-described above is admixed with .the etituent from a partial combustion zone. The partial combustion 5:1.fon'e, for example, ismaintained at a temperature 'with- 'inth'e range of about i800 to 3500 F. at a level where 4the kreaction goes rapidly to completion. At temperatures abovey about k2400 F. the products of combustion comprise carbon monoxide and hydrogen substantially lfree -from methane. AAt the lower temperatures, for example, 'in the tangent-1800 to 2200io F. appreciable amounts of 'methane appear .in the products along with hydrogen and 'carbonmonoxida vThe amount and'preheat temperature of the oil dispersion stream are adjusted such that the .combined stream -ofoil`dispersionand partial combustion pro'ductsis at a temperature yWithin the range of about 1000 to 1800" F. preferably-within the range of about 1200'to 1600" F. The combined -strcarn is contacted at said temperature lwith a crackingcatalyst to effect cracking and reforming of the heavy'oil'components of the stream and .production of a gas-of high calorific value. The catalyst may be disposed as a fixed bed or may be in the form of pulverulent solids. Although substantially less Acarbon `is formediin the process of this invention than'is'formed .in other processes for the gasification of heavy' oils, some carbonaceous deposits form on the catalyst. These deposits may be readily removed from fixed bedsl ofcatavlyst by discontinuing processing, and burning off thecarlbonaceous deposits with oxygen or oxygen-containingA gas streams, for example, air orair diluted vwith lineages. When a fluidized solids catalyst is used, the catalyst may be readily` separated from the product gases and a portion continuously regenerated by passing to a uidized bed regenerator where the carbonaceous deposits are burned with a stream of air.
Pressure in itself is not critical in the dispersion step. The temperature and pressure relationships relating to vaporization are well known. Steam and oil are passed through the dispersion coil at a pressure such that the steam-oil dispersion is discharged at a pressure at least as high as the subsequent gasification zones. A considerable pressure drop takes place in the dispersion coil due to resistance to ow which may be, for example, about 100 pounds per square inch.
In the generation of fuel gas it is desirable to operate the gas generation zone and cracking zone at a superatmospheric pressure, preferably within the range of about 150 to about 1500 pounds per square inch gage. By this means, gas is generated at a pressure high enough for distribution in pipe lines and mains without the necessity of compression. Pressure also exerts an effect on the partial oxidation reactions and the cracking reactions in that pressure favors formation of products of high calorific value.
Carbonaceous fuels generally may be employed in the partial combustion step of the process of this invention. For example, pulverized coal may be gasied by partial combustion with oxygen to provide a stream of carbon monoxide and hydrogen at temperatures in the range of about 1800 to 3500 F. In any event, the heavy oil dispersion prepared as described above is employed in the cracking step of the process of this invention.
An advantage of the process of this invention is that the tendency of heavy hydrocarbon oils to form carbonaceous deposits on the catalyst when employing these oils for catalytic gasification is substantially reduced. The uniform dispersion of oil in steam employed in this process avoids the formation of carbonaceous deposits caused by overcracking which occurs as a result of irregular wetting of catalyst by droplets of oil. The tendency of oil to form carbonaceous deposits during heating is avoided by my method of heating the oil dispersion since only a part of the heating is effected in tubular heaters and the nal increase to cracking temperature is effected by injecting the dispersion into hot synthesis gas. Further, conducting `the cracking reaction in the presence of a gas comprising carbon monoxide and hydrogen tends to suppress the formation of carbonaceous deposits.
Another advantage of this process is that steam-oil dispersions may be readily formed at superatmospheric pressures, for example about 100 to 1500 pounds per square inch. Dispersions formed in accordance with the method of this process permit the uniform distribution of charge components throughout a catalytic reactor equvalent to the distribution of completely vaporized charge oils. Accordingly this method provides an improved means to charge a heavy oil to a catalytic reactor under pressures at which the heavy oil could not be vaporized without cracking.
The accompanying Figure I diagrammatically illustrates one form of the process of this invention. Figure II illustrates another form of the process of this invention. Although the drawings illustrate arrangements of the apparatus in which the process of this invention may be practiced, it is not intended to limit the invention to the particular apparatus or materials described.
Figure I illustrates a form of the process of this invention in which a dispersion of a heavy oil in steam is formed, a part of said dispersion is subjected to partial combustion and another part of said dispersion is admixed with the products of partial combustion and the combined stream contacted with cracking catalyst at cracking temperatures to produce a gas of high calorific value. Water is introduced into the system by pump which feeds water to heating coil 11 in heater 12 where the water is converted to steam. The steam produced in coil 11 is discharged through line 13. Heavy oil from an external source not shown is pumped at a controlled rate by pump 15 through line 16 and is combined with the stream from line 13 inline 17. Pumps 10 and 15 for water and oil respectively permit accurate proportioning of the steam and oil. The mixture of oil and steam, which is at iirst rather crude, is developed into an intimate dispersion af oil particles in steam by passage through a long tubular zone at relatively high velocity, preferably in excess of 50 feet per second, so that the highly turbulent ow thoroughly and evenly disperses the oil droplets in the steam. In the form of the process illustrated in Fig. I, the steam-oil mixture passes through heating coil 18 in heater 19. The oil is continuously injected into the stream of steam in desired proportions and subjected in heating coil 18 to a ternperature within the range of about 300 to l000 F. A part of the resulting steam-oil dispersion passes through lines 21 and 22, ilow control valve 23 and line 24 to burner 26 where it is mixed with oxygen from line 27 and discharged directly into gas generator 2S. Oxygen is introduced through line 27 into burner 26 at a rate controlled by regulator 29. A suitable burner for the partial combustion of oil with oxygen is described in the copending application of Leon P. Gaucher, Serial Number 266,840, tiled January 17, 1952, now Patent Number 2,810,433.
The generator 2S comprises a pressure vessel 30 provided with a suitable refractory and heat insulating lining 31 enclosing a compact, unpacked reaction chamber. Products of reaction ow through outlet 32 which cornmunicate with cracking reactor 33. Another part of the steam-oil dispersion in line 21 passes through line 34, regulator 36 and line 37 and is continuously injected into gas generator outlet 32. The hot product gases leaving generator 28 at substantially the temperature of the generator, in the range of about 1800 to 3500 F., are continuously contacted with steam-oil dispersion from line 37 to form a combined stream at a temperature Within the range of about 1000 to l600 F. and the combined stream passes into cracking reactor 33.
Cracking reactor 33 comprises a pressure vessel 38 in which one or more beds of cracking catalyst 39 are disposed. Any of the well-known cracking catalysts may be used in the process of this invention. Iron group metal catalysts and bauxite, for example, are suitable; nickel catalysts or catalysts containing nickel and chromium are preferred. Cracking of the heavy oil and reaction of the synthesis gas in the combined stream to produce a high B.t.u. gas is effected at a temperature within the range of about 1000 to 1600" F. and at a pressure within the range of about to 1500 pounds per square inch. Products are withdrawn from reactor 33 as the product gas of this process and are dicsharged for distribution or use not shown.
Although the use of the steam-oil dispersion of this process materially reduces the amount of carbonaceous deposits formed on the catalyst, it is necessary to periodically discontinue processing and remove said carbonaceous deposits. Processing is discontinued by closing regulators 23, 29, 36 and 42. Air, from an external source not shown, is then introduced through line 43 and regulator 44 to line 37. Air then passes through reactor 33 and burns the carbonaceous deposit off of the catalyst in bed 39. Flue gas is withdrawn through vent line 46 and regulator 47. After regeneration of the catalyst, regulators 44 and 47 are closed, and processing resumed by opening regulators 23, 29, 36 and 42.
Figure II illustrates a form of the process of this invention in which coal is gasiiied by partial combustion with oxygen to form a gas comprising carbon monoxide and hydrogen, a steam-oil dispersion is formed as described heretofore, the partial combustion products and steam-oil dispersion are admixed and the combined stream is cracked in the presence of a uidized solids catalyst to form heating gas of high caloriiic value.
Crushed coal from an externalsource notlshown is fed into `mixer '51 operated at atmospheric pressure wherein it is admixed with sufficient water from line 52 to form a iiuid slurry. From the mixer 51 the slurry is passed through line 53 into a thickener V54. Excess water is eliminated from the slurry in thickener 54 andV recycled tothe mixer in line 56. Resulting slurry containing only su'icient water to render it tiuid is -wi-thdrawn from thickener`54 through line 57 and charged at elevated pressure by means of pump 58 through line 59 to heating coil 61 in heater 62.
The water is vaporized in the heater dispersng the powdered coal in steam. The dispersion is passed through line 63 into separator 64 where excess steam is withdrawn for heating or other uses not shown through line 66 and regulator 67. Steam-coal dispersion is withdrawn from separator 64 through line 68 and is discharged into generator 69 Ythrough a suitable burner 71. Oxygen is admitted to -burner7 1 through line 72 to maintain the temperature in'thegenerator within the range of 2200 to 3500 F., preferably in the range of about 2200 to 2800 F. Generator69 may comprise a steel shell 73 designed to withstand the internal operating pressure which may be within the range of about 100 to 1500 pounds per square inch. `The gas generator section islined with a suitable 'refractory 74 to withstand the high temperatures generated within the gas generation zone and to protect the shell from overheating. A partition 76 divides the vessel into two separate zones, the gas generation zone 69 and a slag separator or slag pot 77. Product gases from the gas generator pass into the slag pot where hot gases are separated and withdrawn through line 78 and the slag falls to the bottom of the slag pot and is quenched by water introduced through line 79. Solidied slag and water are withdrawn fordisposal through line 81.
Water is introduced through pump 79 and line 81 into heating coil 82 in heater 83 to generate steam. Steam from heating coil 82 discharges through line 84. Heavy oil from an external source not shown is pumped by pump 86 through line 87 and combined with the steam in line 84. The mixture of steam and oil is passed through line 88 to heating coil 89 in heater 91. The intimate dispersion of oil in steam formed by passage through heating coil 89 discharges through line 92 and is combined with the hot gases in line 78 to form a combined stream in line 93 at a temperature within the range of about 1000 to 1600 F. The combined stream in line 93 is contacted with regenerated catalyst from line 94 and is passed through line 96 and inlet cone 97 to cracking reactor 98. A uidized bed of bauxite cracking catalyst 99 is maintained in reactor 98. The combined stream of oil-steam dispersion and partial combustion products is cracked in reactor 98 at 1400 F. and 300 pounds per square inch pressure to form high B.t.u. gas which passes through cyclone separator 1011 and outlet line 102 for external use not shown. In the course of the cracking reaction a carbonaceous deposit forms on the catalyst. This carbonaceous deposit is continuously removed by withdrawing a portion of the catalyst from cracking reactor 98 through sandpipe 103 and regulator 104 for regeneration. Air from compressor 106 is discharged through line 107 to entrain catalyst from standpipe 103 and transfer it to regeneraftor 10S through transfer line 109 and regenerator inlet cone 111. A uidized bed of catalyst 112 is maintained in regenerator 108 and the carbonaceous deposit on the catalyst is lremoved by combustion. Flue gas passes through cyclone separator 113 and is discharged through line 114 to the atmosphere. Regenerated catalyst is withdrawn from regenerator 108 through standpipe 94 and regulator 116 for recycle to the cracking reactor.
Example A reduced crude yoil characterized by a gravity of 14.4 API, a furol viscosity of 200 seconds at`122 F., an ash content of 0.1 weight percent and an ultimate analysis of 85.1 weight percent carbon, 11.0 weight percent hydrogen and 3.9 weight percent sulfur is converted toa high B.t.u. fuel gas by the process of this invention. Steam is generated at a Irate of 12,668 pounds per hour and is admixed with 25,852 pounds per hour of the aforesaid oil preheated to a temperature of 220 F. The mixture at a pressure of 1000 pounds per square inch is passed through a heating coil at a velocity of 55 feet per second wherein the temperature is raised to 750 F. thereby generating a mist-like dispersion of oil in steam. Eighteen thousand two hundred and fifty-six pounds per hour of said dispersion comprising 12,252pounds per hour of oil and 6,004 pounds per hour of steam are subjected to partial combustion with 13,700 pounds per hour of percent oxygen at a temperature of 2500 F. and at a pressure of 475 .pounds per square inch to form 618,000 cubic feet per hourof agas having a heating value of 302 B.t.u. percubic foot (dry basis).
Gas from the partial combustion zone at substantially the temperature of the partial combustion zone is admixed with 20,264 pounds per hour of the steam oil dispersion prepared above. The resulting mixture at a temperature of l,580 F. `and at substantially the pressure of the partial combustion zone is passed through a xed bed of 15.9 cubic feet of a nickel cracking catalyst.-v Eight hundred sixty eight thousand cubic feet per hour of a fuel gas having a heating value of 575 B.t.u. per cubic foot (dry basis) are produced.
Obviously, many modifications and variations 'of the invention as hereinbefore set forth may be made without departing from the spirit and scope thereof and, therefore, only such limitations should be imposed as are indicated in the appended claims.
I claim:
l. A process for the generation of a fuel gas of high a stream of steam and subjecting the resulting mixture of oil and steam to high turbulence effecting dispersion of the oil in the steam while maintaining a portion of the oil in the liquid phase, contacting said combined stream with a cracking catalyst under cracking conditions including a temperature within said range of 1000 to 1600 F., and recovering a composite gas of relatively high heating value as a product of the process.
2. A process for the conversion of a heavy oil to fuel y gas of high calorilic value which comprises introducing a heavy oil into a stream of steam, subjecting `the resulting mixture of oil and steam to high turbulence effecting dispersion of said oil in steam while maintaining at least a portion of said oil in a liquid phase, introducing a part of said dispersion in admixture with oxygen into a partial combustion zone, effecting partial combustion of said oil to form a gas comprising carbon monoxide and hydrogen at a temperature within the range of about 1800 to 3500 F., admixing with said hot gas a part of said dispersion to form a combined stream at a temperature within the range of about 1000 to 1600 F., contacting said'combined stream at said temperature with a cracking catalyst, and recovering a composite gas of relatively high heating Value as a product of the process.
3. The process of claim 1 wherein the amount of steam employed to form said dispersion is within the range of about 20 to about 300 percent by weight of the weight of the oil.
4. The process of claim 2 wherein the dispersion of said oil s developed by highly turbulent ow of the 7 mixture at a temperature within the range of about 300 to 1000 F.
5. The process of claim 2 wherein said cracking catalyst comprises an iron group metal.
6. The process of claim 2 wherein said cracking catalyst comprises nickel.
7. The process of claim 2 wherein said combined stream is contacted with said catalyst at a pressure within the range of about 100 `to 1500 pounds per square inch gauge.
8. A process for the generation of a fuel gas of high caloric value which comprises subjecting a carbonaceous fuel to partial combustion to form a gas comprising carbon monoxide and hydrogen at a temperature within the range of about 1800 to 3500 F. and at a pressure within the range of about 100 to 1500 pounds per square inch, mixing said gas comprising carbon monoxide and hydrogen with a dispersion of heavy oil in steam to form a combined stream at a temperature Within the range of 1000 to 1600 IF., said dispersion of heavy oil in steam being formed by introducing a heavy oil into a stream of steam in proportion within the range of about 20 to 300 percent by weight of steam basis the weight of heavy oil and passing the resulting mixture of oil and steam at a velocity in excess of 20 feet per second through a tubular conduit having a length at least 100 times its inside diameter effecting dispersion of said oil in said steam while maintaining a portion of said oil in the liquid phase, contacting said combined stream with an iron group metal cracking catalyst at a temperature within the range of about 1000 to 1600 F., and recovering a composite gas of relatively high heating value as product of the process.
9. The process of claim 8 wherein said mixture of oil and steam is subjected to heating in at least a portion of said tubular conduit to a temperature within the range of about 300 to 1000 F.
10. The process of claim 8 wherein said iron group metal comprises nickel.
11. The process of claim 8 wherein said combined stream is contacted with said catalyst at a pressure within the range of about to 1500 pounds per square inch.
References Cited in the le of this patent UNITED STATES PATENTS 554,236 Browne 2- Feb. 11, 1896 1,228,818 Pictet June 5, 1917 2,524,840 Shapleigh Oct. 10, 1950 2,539,434 Keith Jan. 30, 1951 2,639,982 Kalbach May 26, 1953 2,692,193 Reisz Oct. 19, 1954 2,793,104 Rees May 21, 1957 2,809,104 Strasser et al. Oct. 8, 1957 2,828,196 Glover et al. Mar. 25, 1958

Claims (1)

1. A PROCESS FOR THE GENERATION OF A FUEL GAS OF HIGH CALORIFIC VALUE WHICH COMPRISES SUBJECTING A CARBONACEOUS FUEL TO PARTIAL COMBUSTION TO FORM A GAS COMPRISING CARBON MONOXIDE AND HYDROGEN AT A TEMPERATURE WITHIN THE RANGE OF ABOUT 1800 TO 3500*F., MIXING SAID GAS WITH A DISPERSION OF HEAVY OIL IN STEAM TO FORM A COMBINED STREAM AT A TEMPERATURE WITHIN THE RANGE OF ABOUT 1000 TO 1600*F., SAID DISPERSION OF HEAVY OIL IN STREAM BEING FORMED BY INTRODUCING A HEAVY OIL INTO A STREAM OF STEAM AND SUBJECTING THE RESULTING MIXTURE OF OIL AND STEAM TO HIGH TURBULENCE EFFECTING DISPERSION OF THE OIL IN THE STREAM WHILE MAINTAINING A PORTION OF THE OIL IN THE LIQUID PHASE, CONTACTING SAID COMBINED STREAM WITH A CRACKING CATALYST UNDER CRACKING CONDITIONS INCLUDING A TEMPERATURE WITHIN SAID RANGE OF 1000 TO 1600*F., AND RECOVERING A COMPOSITE GAS OF RELATIVELY HIGH HEATING VALUE AS A PRODUCT OF THE PROCESS.
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DE1186973B (en) * 1962-02-08 1965-02-11 Metallgesellschaft Ag Process for the continuous catalytic, hydrogenative cleavage of liquid hydrocarbons to form high-temperature gases
US3202603A (en) * 1963-08-16 1965-08-24 Hydrocarbon Research Inc Hydrocracking of high boiling hydrocarbon oils to produce aromatics and fuel gases
US3415634A (en) * 1962-08-03 1968-12-10 Gas Council Treatment of hydrocarbon containing oils
US3476534A (en) * 1967-09-26 1969-11-04 United Aircraft Corp Hydrogen generator including desulfurization with low pressure hydrogen feedback
US3524819A (en) * 1967-03-03 1970-08-18 Lummus Co Steam reforming of hydrocarbons
US3726654A (en) * 1970-03-17 1973-04-10 Metallgesellschaft Ag Process for gasifying heavy hydrocarbons
US4048091A (en) * 1974-10-11 1977-09-13 Centro Sperimentale Metallurgico S.P.A. Process for the preparation of reducing gases
EP0118041A2 (en) * 1983-02-04 1984-09-12 Union Carbide Corporation The method of supplying soot-free products from the partial oxidation of hydrocarbon to the fuel stream of the ACR process
US4854943A (en) * 1988-01-14 1989-08-08 Metallgesellschaft Aktiengesellschaft Process of producing a gas which is rich in carbon monoxide by a cracking of hydrocarbons
US5433760A (en) * 1993-05-13 1995-07-18 Shell Oil Company Method of quenching synthesis gas
EP1624041A1 (en) * 2004-08-03 2006-02-08 Hitachi, Ltd. System for reforming heavy oil , method thereof, and combined cycle power system
US20060185368A1 (en) * 2005-02-24 2006-08-24 Hirokazu Takahashi Gas turbine system burning heavy-oil modified fuel and method of operating same
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US3415634A (en) * 1962-08-03 1968-12-10 Gas Council Treatment of hydrocarbon containing oils
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US3524819A (en) * 1967-03-03 1970-08-18 Lummus Co Steam reforming of hydrocarbons
US3476534A (en) * 1967-09-26 1969-11-04 United Aircraft Corp Hydrogen generator including desulfurization with low pressure hydrogen feedback
US3726654A (en) * 1970-03-17 1973-04-10 Metallgesellschaft Ag Process for gasifying heavy hydrocarbons
US4048091A (en) * 1974-10-11 1977-09-13 Centro Sperimentale Metallurgico S.P.A. Process for the preparation of reducing gases
EP0118041A2 (en) * 1983-02-04 1984-09-12 Union Carbide Corporation The method of supplying soot-free products from the partial oxidation of hydrocarbon to the fuel stream of the ACR process
EP0118041A3 (en) * 1983-02-04 1986-04-16 Union Carbide Corporation The method of supplying soot-free products from the partial oxidation of hydrocarbon to the fuel stream of the acr process
US4854943A (en) * 1988-01-14 1989-08-08 Metallgesellschaft Aktiengesellschaft Process of producing a gas which is rich in carbon monoxide by a cracking of hydrocarbons
US5433760A (en) * 1993-05-13 1995-07-18 Shell Oil Company Method of quenching synthesis gas
EP1624041A1 (en) * 2004-08-03 2006-02-08 Hitachi, Ltd. System for reforming heavy oil , method thereof, and combined cycle power system
US20060057059A1 (en) * 2004-08-03 2006-03-16 Koji Nishida System for reforming heavy oil, method therefor, and combined cycle power system
US7658078B2 (en) 2004-08-03 2010-02-09 Hitachi, Ltd. System for reforming heavy oil, method therefor, and combined cycle power system
US20060185368A1 (en) * 2005-02-24 2006-08-24 Hirokazu Takahashi Gas turbine system burning heavy-oil modified fuel and method of operating same
US7707816B2 (en) * 2005-02-24 2010-05-04 Hitachi, Ltd. Gas turbine system burning heavy-oil modified fuel and method of operating same
US20080253944A1 (en) * 2007-04-13 2008-10-16 Battelle Memorial Institute Method and system for introducing fuel oil into a steam reformer with reduced carbon deposition
WO2008127911A2 (en) * 2007-04-13 2008-10-23 Battelle Memorial Institute Method and system for introducing fuel oil into a steam reformer with reduced carbon deposition
WO2008127911A3 (en) * 2007-04-13 2009-02-12 Battelle Memorial Institute Method and system for introducing fuel oil into a steam reformer with reduced carbon deposition
US7862633B2 (en) 2007-04-13 2011-01-04 Battelle Memorial Institute Method and system for introducing fuel oil into a steam reformer with reduced carbon deposition

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