US3018309A - Pyrolytic conversion of paraffins - Google Patents
Pyrolytic conversion of paraffins Download PDFInfo
- Publication number
- US3018309A US3018309A US841380A US84138059A US3018309A US 3018309 A US3018309 A US 3018309A US 841380 A US841380 A US 841380A US 84138059 A US84138059 A US 84138059A US 3018309 A US3018309 A US 3018309A
- Authority
- US
- United States
- Prior art keywords
- feed
- hydrocarbon
- reaction zone
- steam
- zone
- 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
Links
- 238000006243 chemical reaction Methods 0.000 title claims description 46
- 239000004215 Carbon black (E152) Substances 0.000 claims description 26
- 229930195733 hydrocarbon Natural products 0.000 claims description 26
- 150000002430 hydrocarbons Chemical class 0.000 claims description 25
- 239000000203 mixture Substances 0.000 claims description 12
- 238000010791 quenching Methods 0.000 claims description 12
- 239000000567 combustion gas Substances 0.000 claims description 11
- 238000000034 method Methods 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 230000008021 deposition Effects 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 229930195735 unsaturated hydrocarbon Natural products 0.000 claims description 5
- 239000007800 oxidant agent Substances 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical class [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 2
- 238000004326 stimulated echo acquisition mode for imaging Methods 0.000 claims 3
- -1 OLEFIN HYDROCARBON Chemical class 0.000 claims 1
- 239000012188 paraffin wax Substances 0.000 claims 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 17
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 16
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 12
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 11
- 239000005977 Ethylene Substances 0.000 description 11
- 238000002485 combustion reaction Methods 0.000 description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 239000001294 propane Substances 0.000 description 6
- 239000001273 butane Substances 0.000 description 5
- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 5
- 125000001931 aliphatic group Chemical group 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 239000003480 eluent Substances 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000035484 reaction time Effects 0.000 description 4
- 230000003247 decreasing effect Effects 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 239000011819 refractory material Substances 0.000 description 2
- 229930195734 saturated hydrocarbon Natural products 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- PZBPKYOVPCNPJY-UHFFFAOYSA-N 1-[2-(allyloxy)-2-(2,4-dichlorophenyl)ethyl]imidazole Chemical compound ClC1=CC(Cl)=CC=C1C(OCC=C)CN1C=NC=C1 PZBPKYOVPCNPJY-UHFFFAOYSA-N 0.000 description 1
- 102100024482 Cell division cycle-associated protein 4 Human genes 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 241000948258 Gila Species 0.000 description 1
- 101000980898 Homo sapiens Cell division cycle-associated protein 4 Proteins 0.000 description 1
- 101150079463 NBL1 gene Proteins 0.000 description 1
- 241001387976 Pera Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 239000010431 corundum Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052863 mullite Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052851 sillimanite Inorganic materials 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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
-
- 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
- C10G2400/20—C2-C4 olefins
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S585/00—Chemistry of hydrocarbon compounds
- Y10S585/919—Apparatus considerations
- Y10S585/921—Apparatus considerations using recited apparatus structure
- Y10S585/924—Reactor shape or disposition
- Y10S585/925—Dimension or proportion
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S585/00—Chemistry of hydrocarbon compounds
- Y10S585/949—Miscellaneous considerations
- Y10S585/95—Prevention or removal of corrosion or solid deposits
-
- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S585/00—Chemistry of hydrocarbon compounds
- Y10S585/949—Miscellaneous considerations
- Y10S585/955—Specified mixing procedure
Definitions
- the invention is an improvement in the process of my U.S. Patent 2,750,434, issued June 12, 1956.
- the process disclosed and claimed therein comprises pyrolyzing hydrocarbon feed stocks at temperatures in the range of about 1300 to 3500 F. by introducing a preheated hydrocarbon feed axially into a first cylindrical reaction zone of greater diameter than its length contiguous to and coaxial with a secondY cylindrical reaction zone of lesser diameter than the first zone and of greater length than diameter; injecting tangentially into the first reaction zone a combustible mixture of gaseous fuel and oxidant, such as O2 or air; and burning the mixture to form hot combustion gases for heating the feed; passing the feed, initially surrounded by a helically moving annular blanket of said combustion gases, into the second reaction zone, whereby the feed is heated by the combustion gases to a temperature in the range of 1300 to 3500 F.
- an object of the invention to provide an improved process for pyrolytically converting hydrocarbon feed stocks containing parans to less saturated hydrocarbons with increased yield of unsaturates and higher concentrations thereof in the reaction efuent. Another object is to provide a pyrolytic process for converting hydrocarbon feed stocks to less saturated products with less formation of coke in the reaction system and particularly in the reactor and in the quench chamber adjacent the eluent end of the reaction system. Another object is to reduce coking in a precracking furnace and increase the unsaturates produced therein. Other objects of the invention will become apparent upon consideration of the aompanying disclosure.
- the invention comprises incorporating in the feed to the precracking furnace an amount of steam in the range of about 10 to 125 volume percent of the hydrocarbon feed and preheating the mixture to a temperature in the range of 1000 to 1600 F. so as to crack and upgrade a substantial proportion of the hydrocarbon feed, and passing the precracked feed into a reactor of the character described and under the reaction conditions set forth in the aforesaid patent.
- FIGURE l is a transverse sectional view taken on the line 1-1 of FIGURE 2
- FIGURE 2 is a cross-sectional view of the furnace taken on the line 2-2 of FIGURE 1.
- an elongated reaction zone l. is lined with highly refractory material 12, such as corun dum, silica, mullite, zirconia, or sillimanite brick, or other similar suitable materials resistant to high temperatures developed in the reactor.
- highly refractory material 12 such as corun dum, silica, mullite, zirconia, or sillimanite brick, or other similar suitable materials resistant to high temperatures developed in the reactor.
- a combustion zone 14 Upstream from and contiguous to reaction zone 10 is a combustion zone 14, axial with zone 10, also lined with refractory material 12.
- Lining 12 is surrounded by a layer of insulating material 16 and the whole is sheathed in a steel shell 18.
- Combustion chamber ⁇ 14 should have a relatively large diameter in comparison to "its length while the reverse is true of reaction chamber 10.
- a feed inlet tube 20 is arranged axially so that hydrocarbon feed introduced therethru passes axially thru both chambers 14 and 10.
- a coaxial larger conduit 22 for introducing oxygen or air to the axial feed when this is desired.
- the arrangement of conduits 20 and 22 defines an annular space thru which oxygen or air may be passed into tube 20 thru holes therein (not shown) so that the fuel and air mixture may be passed axially into chamber 14.
- a cooling jacket 24 surrounds the inner end of injection tube 20 and is connected with an inlet water line 25 and an outlet water line 26. Water is circulated thru the jacket from line 25 along the length of the jacket and back to outlet line 26. This cooling of tube 20 lengthens its life.
- FIGURE 2 shows combustion chamber 14 coaxial with reaction chamber 10 and provided with tangential ports or tunnels 28 spaced 180"V apart.
- the outer end of tho tunnel 30 is of smaller diameter than the inner portion.
- a feed inlet pipe 32 is surrounded by a water jacket 34 of the same or similar construction to jacket 24 provided with inlet and outlet lines 36 and 37, respectively.
- the inlet assembly is positioned so as to inject the feed thru tunnels 30 and 28 into combustion zone 14 where it is burned.
- Each tangential inlet conduit 32 is connected with an oxygen or air supply line 40 and a fuel gas supply line 42. Most of the tangentially introduced fuel gas is burned in tunnels 28 and chamber 14.
- Air line 44 and steam line 45 connect with line 46 leading into preheater 48 containing heating coils 50.
- Line 47 connects the outlet end of heating coil 50 with line 40 leading into feed injection conduit 32.
- these gases may bypass preheater 48 thru line 52.
- a cooling assembly 56 at the eluent end of reaction chamber 10, contiguous and coaxial therewith, comprises a water jacket 58, water-spray 60, water inlet conduit 62 extending thru vthe jacket, a cooling water inlet 64, and a cooling water outlet 66 from jacket space 68.
- Etlluent hot gases from the reactor are quenched in cooling assembly 56 to below reaction temperature and the quenched gases are passed via conduit 70 to conventional separation means 72 where acetylene is removed thru line 74, ethylene thru line 76, other olens thru line 78, aromatics thru line 86, byproduct paraiins thru line 82, heavy residual materials thru line 84, and water thru line 86.
- the axial feed comprising steam and parancontaim ing hydrocarbon materail introduced thru lines 88 and 89, respectively, are introduced to pre-cracking furnace 90 thru line 91 where the hydrocarbon feed is subjected ice to cracking in tube coil 92.
- the partially cracked hot eluent is passed thru line 93 into feed injection tube 20 for injection axially thru combustion chamber 14 into reaction chamber 10.
- this gas may be introduced thru line 94 to preheater 95 and thence into line 96, or it may bypass heater 95 and pass thru line 97 into line 96.
- Operation in accordance with the invention comprises injecting a mixture of natural gas (or other fuel gas) and air or oxygen wherein the amount of oxygen is in the range of 50 to 140 percent and, preferably, 90 to l20 percent of theoretical for complete combustion, is preferably preheated and charged to the tangential burners through burner tubes 32 to provide tunnel temperatures up to 3500' F. and sufficient to heat the axial feed to the desired temperature. It is preferred not to heat the air or oxygen in admixture with the fuel gas because of the explosion hazard.
- the oxygen supply may be heated in admixture with steam, ⁇ in the event steam is utilized in the tangential feed.
- the axial feed comprising hydrocarbon and steam is preheated in heater or tube cracker 90 to convert paraflins to unsaturates before introducing the hot effluent from line 93 into injection tube 20.
- the steam admixed with the feed should be in the range of to 125 volume percent of the hydrocarbon. lt is preferred to maintain the steam in the axial feed in the range of 25 to 100 volume percent of the hydrocarbon.
- This feed is heated preferably to a temperature in the range of 800 to 1600 F. so as to crack and upgrade a substantial proportion of the hydrocarbon in the feed.
- axial hydrocarbon feed may contain unsaturates, it is preferred to utilize aliphatic paratlins because of their relative cheapness.
- lt is recognized that unsaturates convert more readily to ethylene and acetylene, but the cost of these hydrocarbons is substantially greater than the cost of corresponding parains.
- Suitable parains include methane, ethane, propane, butane, pentane, hexane and other available hydrocarbon stocks containing substantial amounts of these parains such as naphtha, kerosene, and gas oils.
- the parafiins may be introduced singly in high concentration or in admixture with each other or with unsaturates.
- the axial feed In passing through reaction zone l0, the axial feed is heated to the desired range to produce the desired acetylene and/or ethylene and the effluent is quenched in quenching means 56 by the water injected through spray and by water circulating through jacket 58.
- the effluent from chamber 10 is quenched to a temperature below reaction temperature which is generally below 800 F.
- the quenched effluent is then passed through line into conventional product separation means 72 from which the various constituents are separated in known manner and recovered as desired.
- reaction time is very short in order to avoid overcracking and decomposition to carbon and hydrogen and is usually in the range of 0.5 to 0.001 second and even less.
- the reaction time depends upon the feed, the temperature in the reaction zone, and the product desired. Reaction time may be calculated in accordance with the equations set forth in my U.S. Patent 2,750,- 434, referred to supra.
- the volume ratio of steam to O2 is in the range of 1:1 to 8:1 and it is preferred to preheat the steam -03 mixture to the range of 800 to 1600 F.
- the axial feed was preheated and cracked by being passed through a tube furnace prior to introduction to the reactor.
- run l no steam was included in the axial feed.
- run 2 the effect of mixing 25 volume percent steam with the butane may be seen.
- concentration of the acetylene in the effluent was about 8 hours in each instance.
- run 3 the volume of steam was doubled but there was no significant improvement in results. However, this run was of only 8 hours duration and it is possible that over longer periods of operation, higher steam concentration may result in further reduction in coking in the quencher.
- run 4 steam was included in the tangential feed and this feed was preheated to 1015 F.
- the acetylene concentration was slightly higher than without air preheat and the yield was slightly lower.
- the composition of the propane feed utilized in the runs predominantly unsatuated hyqmcarbons; .the emuem is as fouowsfrom said second reaction zone is quenched in a quench zone to a temperature below reaction temperature; and Run 5: Percent said unsaturated hydrocarbons are recovered; the im- CaHs 67-8 10 provement comprising including at least 50 volume per- CaHs 0-3 cent of aliphatic paran hydrocarbon in said feed; heatiCiHio 18-7 ing said feed in the preheating step toa temperature in nCiHio 13-2 tha rango of about 10oo to i600' F.
- reaction conditions invention effects improved yields of ethylene and acetylene Pl'OdtlCmg mallmum Ylelds 0f acetylen, including a illfrom relatively cheap'parans and also decreases the 00 pramI0fat1a5t1900 F-,alemallllallled and afylelle carbon deposition in the reactor and in the quench cham- 1S ICCUVeId from the UIlSalll'ttS- ber at the gluem end of the Nador, 9.
- reaction conditions 1 claim; producing maximum yields of ethylene, including a tem l.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US841380A US3018309A (en) | 1959-09-21 | 1959-09-21 | Pyrolytic conversion of paraffins |
| DE19601443014 DE1443014A1 (de) | 1959-09-21 | 1960-09-21 | Pyrolytische Umwandlung von Kohlenwasserstoffen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US841380A US3018309A (en) | 1959-09-21 | 1959-09-21 | Pyrolytic conversion of paraffins |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US3018309A true US3018309A (en) | 1962-01-23 |
Family
ID=25284720
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US841380A Expired - Lifetime US3018309A (en) | 1959-09-21 | 1959-09-21 | Pyrolytic conversion of paraffins |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US3018309A (de) |
| DE (1) | DE1443014A1 (de) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3081257A (en) * | 1960-06-06 | 1963-03-12 | Phillips Petroleum Co | Production of aromatic feedstock for carbon black reactors |
| US3170863A (en) * | 1960-09-30 | 1965-02-23 | Monsanto Co | Hydrocarbon conversion process |
| US3213015A (en) * | 1963-02-25 | 1965-10-19 | Phillips Petroleum Co | Cracking of hydrocarbons with steam or carbon dioxide |
| US3347949A (en) * | 1965-06-15 | 1967-10-17 | Phillips Petroleum Co | Heat recovery in thermal conversion process |
| US4288408A (en) * | 1978-07-07 | 1981-09-08 | L. A. Daly Company | Apparatus for the diacritic cracking of hydrocarbon feeds for the selective production of ethylene and synthesis gas |
| US4929797A (en) * | 1987-11-14 | 1990-05-29 | Mitsubishi Kasei Corporation | Method for producing hydrocarbons having two carbon atoms |
| US4982039A (en) * | 1987-09-03 | 1991-01-01 | University Of Southern California | Conversion of halogenated toxic substances |
| US5942652A (en) * | 1994-09-30 | 1999-08-24 | Institut Français Du Petrole | Ethane pyrolysis |
| WO2001090277A1 (en) * | 2000-05-25 | 2001-11-29 | Shell Internationale Research Maatschappij B.V. | Apparatus and process for vaporizing a heavy hydrocarbon feedstock with steam |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2750434A (en) * | 1953-06-11 | 1956-06-12 | Phillips Petroleum Co | Conversion of hydrocarbons |
| US2750420A (en) * | 1953-04-29 | 1956-06-12 | Phillips Petroleum Co | Conversion of hydrocarbons |
| US2790838A (en) * | 1952-01-16 | 1957-04-30 | Eastman Kodak Co | Process for pyrolysis of hydrocarbons |
-
1959
- 1959-09-21 US US841380A patent/US3018309A/en not_active Expired - Lifetime
-
1960
- 1960-09-21 DE DE19601443014 patent/DE1443014A1/de active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2790838A (en) * | 1952-01-16 | 1957-04-30 | Eastman Kodak Co | Process for pyrolysis of hydrocarbons |
| US2750420A (en) * | 1953-04-29 | 1956-06-12 | Phillips Petroleum Co | Conversion of hydrocarbons |
| US2750434A (en) * | 1953-06-11 | 1956-06-12 | Phillips Petroleum Co | Conversion of hydrocarbons |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3081257A (en) * | 1960-06-06 | 1963-03-12 | Phillips Petroleum Co | Production of aromatic feedstock for carbon black reactors |
| US3170863A (en) * | 1960-09-30 | 1965-02-23 | Monsanto Co | Hydrocarbon conversion process |
| US3213015A (en) * | 1963-02-25 | 1965-10-19 | Phillips Petroleum Co | Cracking of hydrocarbons with steam or carbon dioxide |
| US3347949A (en) * | 1965-06-15 | 1967-10-17 | Phillips Petroleum Co | Heat recovery in thermal conversion process |
| US4288408A (en) * | 1978-07-07 | 1981-09-08 | L. A. Daly Company | Apparatus for the diacritic cracking of hydrocarbon feeds for the selective production of ethylene and synthesis gas |
| US4982039A (en) * | 1987-09-03 | 1991-01-01 | University Of Southern California | Conversion of halogenated toxic substances |
| US4929797A (en) * | 1987-11-14 | 1990-05-29 | Mitsubishi Kasei Corporation | Method for producing hydrocarbons having two carbon atoms |
| US5942652A (en) * | 1994-09-30 | 1999-08-24 | Institut Français Du Petrole | Ethane pyrolysis |
| WO2001090277A1 (en) * | 2000-05-25 | 2001-11-29 | Shell Internationale Research Maatschappij B.V. | Apparatus and process for vaporizing a heavy hydrocarbon feedstock with steam |
| US20020028977A1 (en) * | 2000-05-25 | 2002-03-07 | Krishnamoorthy Chandrasekharan | Apparatus and process for vaporizing a heavy hydrocarbon feedstock with steam |
| AU2001274069B2 (en) * | 2000-05-25 | 2004-05-06 | Shell Internationale Research Maatschappij B.V. | Apparatus and process for vaporizing a heavy hydrocarbon feedstock with steam |
| US6797238B2 (en) | 2000-05-25 | 2004-09-28 | Shell Oil Company | Apparatus and process for vaporizing a heavy hydrocarbon feedstock with steam |
| US20050014986A1 (en) * | 2000-05-25 | 2005-01-20 | Krishnamoorthy Chandrasekharan | Apparatus and process for vaporizing a heavy hydrocarbon feedstock with steam |
| RU2260031C2 (ru) * | 2000-05-25 | 2005-09-10 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Аппарат и способ испарения тяжелого углеводородного перерабатываемого сырья водяным паром |
| US7374663B2 (en) | 2000-05-25 | 2008-05-20 | Shell Oil Company | Process for vaporizing a heavy hydrocarbon feedstock with steam |
Also Published As
| Publication number | Publication date |
|---|---|
| DE1443014A1 (de) | 1969-01-30 |
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