CA1248487A - Vaporizing heavy hydrocarbon feedstocks without coking - Google Patents
Vaporizing heavy hydrocarbon feedstocks without cokingInfo
- Publication number
- CA1248487A CA1248487A CA000458254A CA458254A CA1248487A CA 1248487 A CA1248487 A CA 1248487A CA 000458254 A CA000458254 A CA 000458254A CA 458254 A CA458254 A CA 458254A CA 1248487 A CA1248487 A CA 1248487A
- Authority
- CA
- Canada
- Prior art keywords
- heavy hydrocarbon
- heated
- temperature
- heavy
- hydrogen
- 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
Links
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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
-
- 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
- C10G7/00—Distillation of hydrocarbon oils
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
A method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters and is useful in a process for upgrading and/or converting the heavy hydrocarbon to lighter products, such as in a thermal hydrodealkylation process. In the method, a heavy hydrocarbon feedstock material is heated to a temperature below its coking point, then mixed with hydrogen-rich gas heated to a temperature sufficient so that upon mixing with the hydrocarbon feedstock the latter is heated and vaporized without forming coke. Alternatively, the heavy hydrocarbon feedstock can be fractionated to provide a light IBP-550°F
liquid fraction, and a heavy 550-850°F liquid fraction. The light fraction is mixed with hydrogen-rich gas and heated to a temperature sufficiently high so that upon being mixed with the heavy liquid fraction the latter is heated through its dry point and vaporized without coking. The resulting vaporized hydrocarbon material is usually further heated before being fed to a reaction step, such as a hydrodealkylation reaction to produce a hydrodealkylated product.
A method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters and is useful in a process for upgrading and/or converting the heavy hydrocarbon to lighter products, such as in a thermal hydrodealkylation process. In the method, a heavy hydrocarbon feedstock material is heated to a temperature below its coking point, then mixed with hydrogen-rich gas heated to a temperature sufficient so that upon mixing with the hydrocarbon feedstock the latter is heated and vaporized without forming coke. Alternatively, the heavy hydrocarbon feedstock can be fractionated to provide a light IBP-550°F
liquid fraction, and a heavy 550-850°F liquid fraction. The light fraction is mixed with hydrogen-rich gas and heated to a temperature sufficiently high so that upon being mixed with the heavy liquid fraction the latter is heated through its dry point and vaporized without coking. The resulting vaporized hydrocarbon material is usually further heated before being fed to a reaction step, such as a hydrodealkylation reaction to produce a hydrodealkylated product.
Description
-- ~Z48g87 VAPORIZING HEAVY~HYDROCARBON FEEDSTOCKS WITHOUT COKING
BACKGROUND OF THE INVENTION
The present invention relates to the heating and vaporizing of heavy hydrocarbon feedstock materials without coking. More particularly, it relates to a method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters and is useful in a process for upgrading and/or converting the heavy hydrocarbon to lighter products, such as in a thermal hydrodealkylation process.
One barrier to successful hydrodealkylation of heavy hydrocarbon aromatic materials such as steam cracker tar to produce mono-ring product materials is vaporization of the liquid phase feed material without producing excessive coke formation during the preheating step. It has generally been found that such heavy hydrocarbon liquids when preheated to above about 550~F are susceptible to coking. To overcome ~0 this pxoblem of undesired coke formation during preheating and to permit feeding of heavier vaporized feedstock materials to thermal or catalytic reaction processes, it has been found possible to make use of superheated hydrogen and/or hydrocarbon vapors mixed with the heavy hydrocarbon feed to rapidly heat and vaporize the heavy hydrocarbon liquids to provide a vapor phase material without coking of the heavy hydrocarbon feed material. Although it is known in industry to use preheated hydrogen mixed with feed liquids upstream of a reaction step, such heated hydrogen has apparently not been previously used to vaporize hydrocarbon heavy feedstock materials which contain constituents which are prone to coking in a conventional tubular fired heater preheating step.
SUMMARY OF INVENTION
This invention provides a method for providing a vaporized heavy hydrocarbon feedstock which avoids the 12g~
formation of coke in the feed heaters and is useful in a process for upgrading and/or converting the heavy hydrocarbon to lighter products, such as in a thermal hydrodealkylation process. The method comprises heating a heavy hydrocarbon feedstock to a temperature below its coking temperature, heating hydrogen-rich gas to a temperature sufficiently above the temperature of the heated heavy hydrocarbon feedstock so that upon mixing the heated hydrocarbon feedstock and hydrogen together the heavy hydrocarbon feed material is completely vaporized without forming any coke. In a second embodiment of the invention, a heavy hydrocarbon feedstock is first fractionated into a lighter fraction normally boiling below about 550F and a heavier fraction having a normal boiling range of about 550F to about 850F. The heavier hydrocarbon fraction is heated to a temperature below its coking point, and the lighter fraction and hydrogen-rich gas are heated separately to a temperature below the coking point of the lighter fraction and sufficiently above ' the temperature of the heated heavy hydrocarbon fraction to 210 provide heat content sufficient that upon being mixed with the heavy hydrocarbon fraction the latter is vaporized without forming any coke. Using this invention, the temperature of the mixing chamber wall can be maintained at a significantly lower temperature than would be required for the wall temperature of a tubular type fired preheater for vaporizing the feedstock.
This invention for vaporizing heavy hydrocarbon feedstocks i5 useful at a pressure range of 50-5000 psig. The vaporized hydrocarbon material stream can then be further heated and fed to a reaction step such as hydrodealkylation to produce hydrodealkylated products.
BRIEF DESCRIPTION OF DRAWINGS
FIG. 1 is a flow diagram illustrating a method for vaporizing a heavy hydrocarbon feedstock according to the present invention; and ~248~7 ., - 3 - ~
FIG. 2 is a flow diagram of a second embodiment of the method illustrated in FIG. 1.
DETAILED DESCRIPTION OF INVENTION
In the present invention for vaporizing heavy hydrocarbon feedstocks, so as to avoid formation of coke, hydrogen-rich gas is heated to a temperature sufficient that upon mixing with the heavy hydrocarbon feedstocks will effectively heat same through their dry point and vaporize the heavy feedstock without coking. The heated hydrogen-rich gas is mixed with the heavy feedstock in a suitable mixing step such as a venturi mixer. The temperature of the heated hydrogen-rich gas is much higher than the temperature of the heavy hydrocarbon feed material, and is sufficiently high, such as 900-1250F, that it supplies all the heat needed to vaporize the heavy hydrocarbon liquid feedstock, which normally boils above about 550F and preferably has a boiling - range of 550-650F. Because of the rapid heat transfer which occurs between the mixed streams in the mixing step, this heating method avoids transferring heat from a hot wall to the hydrocarbon feedstock and minimizes the time required to vaporize the heavy feed material and avoids coking of the material.
In a second embodiment of the invention, the hydrogen-rich gas can be premixed with a light hydrocarbon fraction having a normal boiling range of about 400-650F and heated together to a temperature below the coking point of the light hydrocarbon fraction and sufficient that upon mixing with the heavy hydrocarbon feedstock fraction will rapidly heat same through its dry point and completely vaporize the heavy hydrocarbon feedstock without coking of the heavy hydrocarbon feedstock material.
This invention can be used for vaporizing any heavy hydrocarbon feed material for which a vapor phase reaction is required, such as for vaporizing heavy gas oils -- 4 .
and steam cracker tar derived from petroleum, and coal-derived liquids, prior to feeding the vaporized hydrocarbon material to a reaction step such as thermal hydrocracking or hydro-dealkylation to produce hydrodealkylation products. Useful pressure ranges for the invention are 50-5000 psig, and preferably 200-1000 psig.
As shown in the Fig. 1 drawing, a heavy hydrocarbon feedstock material such as heavy gas oil, is provided at 10, pressurized at 11 to at least about 200 psig and heated in furnace 12 to a temperature such as about 560F, which will not produce coke deposits inside the tubes 13 of the furnace.
The heated feedstock stream at 14 is passed to a mixing step at 20. Also, hydrogen-rich gas is provided at 16 and heated in furnace 18 to a temperature well above the temperature of the mixing step 20 and also passed to the mixing step.
Mixing step 20 may comprise any suitable known mixing device which provides complete mixing at relatively high velocities, such as a length of pipe, nozzle or venturi, with , the heavy oil stream 14 preferably being introduced into the throat section of a venturi type mixer device. The heat content provided in hydrogen-rich stream 19 is sufficient to completely vaporize the heavy hydrocarbon feed stream 14, and thus avoids heating the hydrocarbon feedstock through its dry point by contact with a hot metal wall maintained at higher temperature than the feedstock and thereby prevents any coking of the heavy feed material during such heating.
The resulting vaporized material at 21 is further heated in heater 22 to about 1250F and passed to a reaction step 24, such as for a hydrodealkylation process, to produce a product 26.
In an alternative embodiment of the invention, as shown in Fig. 2, a heavy feedstock material such as steam cracker tar is provided at 30 and fed into fractionation tower 32, which is usually maintained at operating conditions of about 200-300F temperature and 1-5 psia pressure. From tower 32, a vapor stream can be withdrawn at 33, a light liquid ;a 4~3 a87 stream normally boiling up to about 550F is withdrawn at 34, a heavy liquid stream having a normal boiling range of 550-850F is withdrawn at 36, and a heavier bottoms material boiling above about 850F is withdrawn at 38.
Light liquid stream 34 is pressurized at 35 to at least about 200 psig, hydrogen-rich gas is added at 40 and heated at 41, and the resulting mixture is heated in heater 42 to a temperature above about 950F and passed as stream 43 to ~ mixing device having a reduced pressure and increased velocity at the throat section. The heavy boiling liquid stream 36 is pressurized at 37 to at least about 200 psig, heated at 46 to a temperature sufficiently low to avoid coking in the tubes of heater 46, such as about 550F, and also passed to mixing step 44. The heat provided in stream 43 is sufficient to vaporize liquid stream 47, so that the resulting mixed stream which emerges at 45 from mixer 44 is completely vaporized.
This vapor stream 45 is then passed through heater 48 for further heating such as to 1200-1250F temperature before passing to reaction step 50, which may preferably be a hydro-dealkylation step. If the feedstock at 30 is a polynuclear aromatic or polyalkylated phenol material, the light liquid stream at 34 can contain mainly alkylated naphthalene material, which is heated with hydrogen-rich gas at heater 42 to a temperature sufficient so that upon being mixed with the heated heavy stream 47, which can be mainly alkylated phenanthrenes, the latter is completely vaporized. The resulting vaporized material is then fed to a hydrodealkylation reaction process step at 50 to produce product at 52.
This invention will be further described by reference to the following examples, which should not be construed as limiting in scope.
To show the method and utility of the present invention, a heavy hydrocarbon feed material such as gas oil normally boiling above about 600F temperature is pressurized
BACKGROUND OF THE INVENTION
The present invention relates to the heating and vaporizing of heavy hydrocarbon feedstock materials without coking. More particularly, it relates to a method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters and is useful in a process for upgrading and/or converting the heavy hydrocarbon to lighter products, such as in a thermal hydrodealkylation process.
One barrier to successful hydrodealkylation of heavy hydrocarbon aromatic materials such as steam cracker tar to produce mono-ring product materials is vaporization of the liquid phase feed material without producing excessive coke formation during the preheating step. It has generally been found that such heavy hydrocarbon liquids when preheated to above about 550~F are susceptible to coking. To overcome ~0 this pxoblem of undesired coke formation during preheating and to permit feeding of heavier vaporized feedstock materials to thermal or catalytic reaction processes, it has been found possible to make use of superheated hydrogen and/or hydrocarbon vapors mixed with the heavy hydrocarbon feed to rapidly heat and vaporize the heavy hydrocarbon liquids to provide a vapor phase material without coking of the heavy hydrocarbon feed material. Although it is known in industry to use preheated hydrogen mixed with feed liquids upstream of a reaction step, such heated hydrogen has apparently not been previously used to vaporize hydrocarbon heavy feedstock materials which contain constituents which are prone to coking in a conventional tubular fired heater preheating step.
SUMMARY OF INVENTION
This invention provides a method for providing a vaporized heavy hydrocarbon feedstock which avoids the 12g~
formation of coke in the feed heaters and is useful in a process for upgrading and/or converting the heavy hydrocarbon to lighter products, such as in a thermal hydrodealkylation process. The method comprises heating a heavy hydrocarbon feedstock to a temperature below its coking temperature, heating hydrogen-rich gas to a temperature sufficiently above the temperature of the heated heavy hydrocarbon feedstock so that upon mixing the heated hydrocarbon feedstock and hydrogen together the heavy hydrocarbon feed material is completely vaporized without forming any coke. In a second embodiment of the invention, a heavy hydrocarbon feedstock is first fractionated into a lighter fraction normally boiling below about 550F and a heavier fraction having a normal boiling range of about 550F to about 850F. The heavier hydrocarbon fraction is heated to a temperature below its coking point, and the lighter fraction and hydrogen-rich gas are heated separately to a temperature below the coking point of the lighter fraction and sufficiently above ' the temperature of the heated heavy hydrocarbon fraction to 210 provide heat content sufficient that upon being mixed with the heavy hydrocarbon fraction the latter is vaporized without forming any coke. Using this invention, the temperature of the mixing chamber wall can be maintained at a significantly lower temperature than would be required for the wall temperature of a tubular type fired preheater for vaporizing the feedstock.
This invention for vaporizing heavy hydrocarbon feedstocks i5 useful at a pressure range of 50-5000 psig. The vaporized hydrocarbon material stream can then be further heated and fed to a reaction step such as hydrodealkylation to produce hydrodealkylated products.
BRIEF DESCRIPTION OF DRAWINGS
FIG. 1 is a flow diagram illustrating a method for vaporizing a heavy hydrocarbon feedstock according to the present invention; and ~248~7 ., - 3 - ~
FIG. 2 is a flow diagram of a second embodiment of the method illustrated in FIG. 1.
DETAILED DESCRIPTION OF INVENTION
In the present invention for vaporizing heavy hydrocarbon feedstocks, so as to avoid formation of coke, hydrogen-rich gas is heated to a temperature sufficient that upon mixing with the heavy hydrocarbon feedstocks will effectively heat same through their dry point and vaporize the heavy feedstock without coking. The heated hydrogen-rich gas is mixed with the heavy feedstock in a suitable mixing step such as a venturi mixer. The temperature of the heated hydrogen-rich gas is much higher than the temperature of the heavy hydrocarbon feed material, and is sufficiently high, such as 900-1250F, that it supplies all the heat needed to vaporize the heavy hydrocarbon liquid feedstock, which normally boils above about 550F and preferably has a boiling - range of 550-650F. Because of the rapid heat transfer which occurs between the mixed streams in the mixing step, this heating method avoids transferring heat from a hot wall to the hydrocarbon feedstock and minimizes the time required to vaporize the heavy feed material and avoids coking of the material.
In a second embodiment of the invention, the hydrogen-rich gas can be premixed with a light hydrocarbon fraction having a normal boiling range of about 400-650F and heated together to a temperature below the coking point of the light hydrocarbon fraction and sufficient that upon mixing with the heavy hydrocarbon feedstock fraction will rapidly heat same through its dry point and completely vaporize the heavy hydrocarbon feedstock without coking of the heavy hydrocarbon feedstock material.
This invention can be used for vaporizing any heavy hydrocarbon feed material for which a vapor phase reaction is required, such as for vaporizing heavy gas oils -- 4 .
and steam cracker tar derived from petroleum, and coal-derived liquids, prior to feeding the vaporized hydrocarbon material to a reaction step such as thermal hydrocracking or hydro-dealkylation to produce hydrodealkylation products. Useful pressure ranges for the invention are 50-5000 psig, and preferably 200-1000 psig.
As shown in the Fig. 1 drawing, a heavy hydrocarbon feedstock material such as heavy gas oil, is provided at 10, pressurized at 11 to at least about 200 psig and heated in furnace 12 to a temperature such as about 560F, which will not produce coke deposits inside the tubes 13 of the furnace.
The heated feedstock stream at 14 is passed to a mixing step at 20. Also, hydrogen-rich gas is provided at 16 and heated in furnace 18 to a temperature well above the temperature of the mixing step 20 and also passed to the mixing step.
Mixing step 20 may comprise any suitable known mixing device which provides complete mixing at relatively high velocities, such as a length of pipe, nozzle or venturi, with , the heavy oil stream 14 preferably being introduced into the throat section of a venturi type mixer device. The heat content provided in hydrogen-rich stream 19 is sufficient to completely vaporize the heavy hydrocarbon feed stream 14, and thus avoids heating the hydrocarbon feedstock through its dry point by contact with a hot metal wall maintained at higher temperature than the feedstock and thereby prevents any coking of the heavy feed material during such heating.
The resulting vaporized material at 21 is further heated in heater 22 to about 1250F and passed to a reaction step 24, such as for a hydrodealkylation process, to produce a product 26.
In an alternative embodiment of the invention, as shown in Fig. 2, a heavy feedstock material such as steam cracker tar is provided at 30 and fed into fractionation tower 32, which is usually maintained at operating conditions of about 200-300F temperature and 1-5 psia pressure. From tower 32, a vapor stream can be withdrawn at 33, a light liquid ;a 4~3 a87 stream normally boiling up to about 550F is withdrawn at 34, a heavy liquid stream having a normal boiling range of 550-850F is withdrawn at 36, and a heavier bottoms material boiling above about 850F is withdrawn at 38.
Light liquid stream 34 is pressurized at 35 to at least about 200 psig, hydrogen-rich gas is added at 40 and heated at 41, and the resulting mixture is heated in heater 42 to a temperature above about 950F and passed as stream 43 to ~ mixing device having a reduced pressure and increased velocity at the throat section. The heavy boiling liquid stream 36 is pressurized at 37 to at least about 200 psig, heated at 46 to a temperature sufficiently low to avoid coking in the tubes of heater 46, such as about 550F, and also passed to mixing step 44. The heat provided in stream 43 is sufficient to vaporize liquid stream 47, so that the resulting mixed stream which emerges at 45 from mixer 44 is completely vaporized.
This vapor stream 45 is then passed through heater 48 for further heating such as to 1200-1250F temperature before passing to reaction step 50, which may preferably be a hydro-dealkylation step. If the feedstock at 30 is a polynuclear aromatic or polyalkylated phenol material, the light liquid stream at 34 can contain mainly alkylated naphthalene material, which is heated with hydrogen-rich gas at heater 42 to a temperature sufficient so that upon being mixed with the heated heavy stream 47, which can be mainly alkylated phenanthrenes, the latter is completely vaporized. The resulting vaporized material is then fed to a hydrodealkylation reaction process step at 50 to produce product at 52.
This invention will be further described by reference to the following examples, which should not be construed as limiting in scope.
To show the method and utility of the present invention, a heavy hydrocarbon feed material such as gas oil normally boiling above about 600F temperature is pressurized
2~8413~
to about 650 psia pressure and heated to a temperature at least 600F but below which vaporization or any coking of the feed occurs. The heated feed material is then vaporized by being mixed with a hydroyen-rich stream heated to a temperature sufficiently above the mixing temperature to have a heat content sufficient that upon being mixed with the heavy liquid feed will completely vaporize the feed without coking. The molar flow ratio of hydrogen-rich gas to feed liquid is about 13, and the hydrogen stream contains 90% hydrogen and 10%
methane. Results of the heating and mixing steps for various hydrocarbon feedstock fractions are shown in Table 1.
VAPORIZING HYPROCARBON FEEDSTOCK
BY MIXING WITH HEATED HYDROGEN
Liquid Feedstock Liquid Feed H2 Gas Mixing Avg.BP, F Temp, F Temp, F Temp, F
' 650 600 1125 735 It is seen that the heavy hydrocarbon feed materials having average boiling points between 600 and 700F can be heated and completely vaporized without coking by being mixed with a hydrogen-rich gas stream heated to a higher temperature but not exceeding about 1250F to provide a hydrocarbon vapor material.
A heavy hydrocarbon feed material such as steam cracker tar is fractionated into at least a light fraction having a normal boiling lange OL 300-550F and a heavy fraction having a boiling range of 550-850F. The heavy hydrocarbon fraction is heated to a temperature below its coking point and passed to a mixing step. The light fraction stream is mixed ~248~87 - 7 - ~
with heated hydrogen-rich gas and the resulting mixed stream is heated to a temperature higher than that of the heavy fraction and such as to provide a heat content sufficient that upon mixing the two preheated hydrocarbon streams together the heavy hydrocarbon stream is completely vaporized without any coking. Results of the heating and mixing steps for various hydrocarbon feedstocks at 650 psi using 13 moles hydrogen, 1 mole light hydrocarbon fraction and 1 mole heavy hydrocarbon fraction feed are shown in Table 2.
VAPORIZING HEAVY HYDROCARBON FRACTION BY MIXING
WITH HEATED HYDROGEN AND LIGHT HYDROCARBON FRACTION
Heavy Light Liquid Liquid FeedstockLiquid Feed and H2 Gas Mixing*
Avg.BP, F Temp, F Temp, F Temp, F
~ 700 600 1000 820 *Temperatures are + 3pF.
.
It is seen that the heavy hydrocarbon feedstocks having initial normal boiling points between about 600-700F
can be heated and completely vaporized without coking by being mixed with a light hydrocarbon liquid fraction and hydrogen-rich gas mixture heated to a temperature sufficiently above the mixing temperature, but not exceeding about 1000F to heat and vaporize the heavy feedstock and provide a hydrocarbon vapor material.
Although this invention has been described broadly and with reference to certain embodiments thereof, it will be understood that modifications and variations to the method can be made within the spirit and scope of the invention, which is defined by the following claims.
to about 650 psia pressure and heated to a temperature at least 600F but below which vaporization or any coking of the feed occurs. The heated feed material is then vaporized by being mixed with a hydroyen-rich stream heated to a temperature sufficiently above the mixing temperature to have a heat content sufficient that upon being mixed with the heavy liquid feed will completely vaporize the feed without coking. The molar flow ratio of hydrogen-rich gas to feed liquid is about 13, and the hydrogen stream contains 90% hydrogen and 10%
methane. Results of the heating and mixing steps for various hydrocarbon feedstock fractions are shown in Table 1.
VAPORIZING HYPROCARBON FEEDSTOCK
BY MIXING WITH HEATED HYDROGEN
Liquid Feedstock Liquid Feed H2 Gas Mixing Avg.BP, F Temp, F Temp, F Temp, F
' 650 600 1125 735 It is seen that the heavy hydrocarbon feed materials having average boiling points between 600 and 700F can be heated and completely vaporized without coking by being mixed with a hydrogen-rich gas stream heated to a higher temperature but not exceeding about 1250F to provide a hydrocarbon vapor material.
A heavy hydrocarbon feed material such as steam cracker tar is fractionated into at least a light fraction having a normal boiling lange OL 300-550F and a heavy fraction having a boiling range of 550-850F. The heavy hydrocarbon fraction is heated to a temperature below its coking point and passed to a mixing step. The light fraction stream is mixed ~248~87 - 7 - ~
with heated hydrogen-rich gas and the resulting mixed stream is heated to a temperature higher than that of the heavy fraction and such as to provide a heat content sufficient that upon mixing the two preheated hydrocarbon streams together the heavy hydrocarbon stream is completely vaporized without any coking. Results of the heating and mixing steps for various hydrocarbon feedstocks at 650 psi using 13 moles hydrogen, 1 mole light hydrocarbon fraction and 1 mole heavy hydrocarbon fraction feed are shown in Table 2.
VAPORIZING HEAVY HYDROCARBON FRACTION BY MIXING
WITH HEATED HYDROGEN AND LIGHT HYDROCARBON FRACTION
Heavy Light Liquid Liquid FeedstockLiquid Feed and H2 Gas Mixing*
Avg.BP, F Temp, F Temp, F Temp, F
~ 700 600 1000 820 *Temperatures are + 3pF.
.
It is seen that the heavy hydrocarbon feedstocks having initial normal boiling points between about 600-700F
can be heated and completely vaporized without coking by being mixed with a light hydrocarbon liquid fraction and hydrogen-rich gas mixture heated to a temperature sufficiently above the mixing temperature, but not exceeding about 1000F to heat and vaporize the heavy feedstock and provide a hydrocarbon vapor material.
Although this invention has been described broadly and with reference to certain embodiments thereof, it will be understood that modifications and variations to the method can be made within the spirit and scope of the invention, which is defined by the following claims.
Claims (20)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters and is useful in a process for upgrading and/or converting said heavy hydrocarbons, said method comprising:
(a) heating a heavy hydrocarbon feedstock to a temperature at least about 500°F but below its coking point;
(b) heating hydrogen-rich gas to a temperature sufficiently above the temperature of said heated heavy hydro-carbon feedstock so as to provide a heat content sufficient to vaporize said heated heavy hydrocarbon feedstock; and (c) mixing said heated heavy hydrocarbon feedstock together with said heated hydrogen-rich gas and vaporizing the heavy hydrocarbon feedstock to provide a hydrocarbon vapor material without forming coke.
(a) heating a heavy hydrocarbon feedstock to a temperature at least about 500°F but below its coking point;
(b) heating hydrogen-rich gas to a temperature sufficiently above the temperature of said heated heavy hydro-carbon feedstock so as to provide a heat content sufficient to vaporize said heated heavy hydrocarbon feedstock; and (c) mixing said heated heavy hydrocarbon feedstock together with said heated hydrogen-rich gas and vaporizing the heavy hydrocarbon feedstock to provide a hydrocarbon vapor material without forming coke.
2. The method of claim 1, wherein said heavy hydrocarbon feedstock is heated to a temperature of 550-650°F.
3. The method of claim 1, wherein said hydrogen is heated to a temperature of 1000-1250°F.
4. The method of claim 1, wherein the heavy hydrocarbon feedstock is steam cracker tar derived from petroleum.
5. The method of claim 1, wherein the heavy hydrocarbon feedstock is coal-derived liquids.
6. The method of claim 1, wherein said mixing step occurs in a venturi device.
7. The method of claim 1, wherein the mixed and vaporized hydrocarbon material and hydrogen-rich gas are further heated to a temperature above the vaporization tem-perature of said heavy hydrocarbon feedstock.
8. The method of claim 7, wherein said heated mixture of vaporized hydrocarbon material and hydrogen are fed into a hydrodealkylation reaction step to produce a hydrodealkylated product.
9. A method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters useful in a process for upgrading and/or converting said heavy hydrocarbon, said method comprising:
(a) heating a heavy hydrocarbon feedstock to a 550-650°F temperature;
(b) heating hydrogen-rich gas to a 1000-1250°F
temperature to provide a heat content sufficient to vaporize said heated heavy hydrocarbon feedstock;
(c) mixing said heated heavy hydrocarbon fractions together with said heated hydrogen-rich gas and vaporizing the heavy hydrocarbon feedstock to provide a hydrocarbon vapor material without forming coke; and (d) further heating said vaporized hydrocarbon material and hydrogen-rich gas to a temperature not exceeding about 1250°F, and passing a vaporized hydrocarbon material to a reaction step.
(a) heating a heavy hydrocarbon feedstock to a 550-650°F temperature;
(b) heating hydrogen-rich gas to a 1000-1250°F
temperature to provide a heat content sufficient to vaporize said heated heavy hydrocarbon feedstock;
(c) mixing said heated heavy hydrocarbon fractions together with said heated hydrogen-rich gas and vaporizing the heavy hydrocarbon feedstock to provide a hydrocarbon vapor material without forming coke; and (d) further heating said vaporized hydrocarbon material and hydrogen-rich gas to a temperature not exceeding about 1250°F, and passing a vaporized hydrocarbon material to a reaction step.
10. A method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters and is useful in a process for upgrading and/or converting said heavy hydrocarbon feedstock to lighter products, said method comprising:
(a) fractionating a heavy hydrocarbon feedstock into a light fraction having a normal boiling temperature below about 550°F and a heavy fraction having a normal boiling temperature range of about 550 to about 850°F;
(b) heating said heavy hydrocarbon fraction to a temperature at least about 500°F but below its coking point;
(c) heating hydrogen-rich gas and said light hydrocarbon fraction to a temperature sufficiently above the temperature of said heated heavy hydrocarbon fraction to avoid coking the light hydrocarbon fraction and provide a heat content sufficient to vaporize said heavy hydrocarbon fraction;
(d) mixing said heated heavy hydrocarbon fraction together with said hydrogen-rich gas and light hydrocarbon fraction to vaporize the heavy hydrocarbon fraction and provide a hydrocarbon vapor material without forming coke; and (e) further heating said vaporized hydrocarbon material and hydrogen-rich gas to a temperature not exceeding about 1250°F, and passing a vaporized hydrocarbon material to a reaction step.
(a) fractionating a heavy hydrocarbon feedstock into a light fraction having a normal boiling temperature below about 550°F and a heavy fraction having a normal boiling temperature range of about 550 to about 850°F;
(b) heating said heavy hydrocarbon fraction to a temperature at least about 500°F but below its coking point;
(c) heating hydrogen-rich gas and said light hydrocarbon fraction to a temperature sufficiently above the temperature of said heated heavy hydrocarbon fraction to avoid coking the light hydrocarbon fraction and provide a heat content sufficient to vaporize said heavy hydrocarbon fraction;
(d) mixing said heated heavy hydrocarbon fraction together with said hydrogen-rich gas and light hydrocarbon fraction to vaporize the heavy hydrocarbon fraction and provide a hydrocarbon vapor material without forming coke; and (e) further heating said vaporized hydrocarbon material and hydrogen-rich gas to a temperature not exceeding about 1250°F, and passing a vaporized hydrocarbon material to a reaction step.
11. The method of claim 10, wherein said heavy hydrocarbon fraction is heated to a 550-650°F temperature.
12. The method of claim 10, wherein said hydrogen and light hydrocarbon fraction are heated together to a 1000-1250°F temperature.
13. The method of claim 10, wherein said fractionation step occurs at vacuum pressure.
14. The method of claim 10, wherein the heavy hydrocarbon feedstock is steam cracker tar derived from petroleum.
15. The method of claim 10, wherein the heavy hydrocarbon feedstock is coal-derived liquid.
16. The method of claim 10, wherein said mixed and vaporized hydrocarbon fractions and hydrogen-rich gas are further heated to a temperature above the vaporization temperature of said heavy hydrocarbon feedstock.
17. The method of claim 16, wherein said heated mixture of vaporized hydrocarbon feedstock and hydrogen-rich gas are fed into a hydrodealkylation reaction step to produce a hydrodealkylated product.
18. A method for providing a vaporized heavy hydrocarbon feedstock which avoids the formation of coke in the feed heaters useful in a process for upgrading and/or converting said heavy hydrocarbon, said method comprising:
(a) fractionating a heavy hydrocarbon feedstock into a light fraction having a normal boiling temperature below about 550°F and a heavy fraction having a normal boiling temperature range of about 550 to about 850°F;
(b) heating said heavy hydrocarbon fraction to a temperature of 550-650°F;
(c) heating hydrogen-rich gas and said light hydrocarbon fraction to a temperature sufficiently above the temperature of said heated heavy hydrocarbon fraction to avoid coking the light hydrocarbon fraction and to provide a heat content sufficient to vaporize said heavy hydrocarbon fraction;
and (d) mixing said heated heavy hydrocarbon fraction together with said hydrogen-rich gas and light hydrocarbon fraction to completely vaporize the heavy hydrocarbon fraction and provide a hydrocarbon vapor material without forming coke.
(a) fractionating a heavy hydrocarbon feedstock into a light fraction having a normal boiling temperature below about 550°F and a heavy fraction having a normal boiling temperature range of about 550 to about 850°F;
(b) heating said heavy hydrocarbon fraction to a temperature of 550-650°F;
(c) heating hydrogen-rich gas and said light hydrocarbon fraction to a temperature sufficiently above the temperature of said heated heavy hydrocarbon fraction to avoid coking the light hydrocarbon fraction and to provide a heat content sufficient to vaporize said heavy hydrocarbon fraction;
and (d) mixing said heated heavy hydrocarbon fraction together with said hydrogen-rich gas and light hydrocarbon fraction to completely vaporize the heavy hydrocarbon fraction and provide a hydrocarbon vapor material without forming coke.
19. The method of claim 18, wherein said mixed and vaporized hydrocarbon fractions and hydrogen are further heated to a temperature above the vaporization temperature of said heavy hydrocarbon feedstock.
20. The method of claim 19, wherein said further heated mixture of vaporized hydrocarbon feedstock fractions and hydrogen are fed into a hydrodealkylation reaction to produce a hydrodealkylation product.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US52527183A | 1983-08-23 | 1983-08-23 | |
| US525,271 | 1983-08-23 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1248487A true CA1248487A (en) | 1989-01-10 |
Family
ID=24092583
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000458254A Expired CA1248487A (en) | 1983-08-23 | 1984-07-06 | Vaporizing heavy hydrocarbon feedstocks without coking |
Country Status (5)
| Country | Link |
|---|---|
| JP (1) | JPS6055082A (en) |
| CA (1) | CA1248487A (en) |
| DE (1) | DE3426036A1 (en) |
| GB (1) | GB2145426B (en) |
| ZA (1) | ZA844353B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2249051A1 (en) * | 1998-09-29 | 2000-03-29 | Canadian Environmental Equipment & Engineering Technologies Inc. | Process for upgrading crude oil using low pressure hydrogen |
| US6908543B1 (en) | 2000-10-23 | 2005-06-21 | Chevron U.S.A. Inc. | Method for retarding fouling of feed heaters in refinery processing |
| CN108067168A (en) * | 2017-12-13 | 2018-05-25 | 煤炭科学技术研究院有限公司 | Heterogeneous slurry bed system hydrocracking unit and method |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE514529A (en) * | 1951-10-03 | |||
| US3448039A (en) * | 1967-07-19 | 1969-06-03 | Bethlehem Steel Corp | Vaporizing and pretreating aromatic hydrocarbon feed stock without polymerization |
| NL6800273A (en) * | 1968-01-08 | 1969-07-10 | ||
| US3666658A (en) * | 1970-11-23 | 1972-05-30 | Universal Oil Prod Co | Hydroprocessing product separation |
| GB1434018A (en) * | 1972-08-16 | 1976-04-28 | British Gas Corp | Production of fuel gases |
| JPS5829838B2 (en) * | 1975-01-13 | 1983-06-24 | ブリテイツシユ ガス コ−ポレ−シヨン | Method and device for vaporizing liquids mainly composed of hydrocarbons |
| CA1080974A (en) * | 1975-09-18 | 1980-07-08 | Burton E. Moody | Gasification of hydrocarbon feedstocks |
| JPS536968A (en) * | 1976-07-08 | 1978-01-21 | Unitika Ltd | Filtration concentration method |
| US4256565A (en) * | 1979-11-13 | 1981-03-17 | Rockwell International Corporation | Method of producing olefins from hydrocarbons |
| FR2516932B1 (en) * | 1981-11-24 | 1985-07-19 | Inst Francais Du Petrole | PROCESS FOR CONVERTING HEAVY OILS OR OIL RESIDUES INTO GASEOUS AND DISTILLABLE HYDROCARBONS |
-
1984
- 1984-06-08 ZA ZA844353A patent/ZA844353B/en unknown
- 1984-07-06 CA CA000458254A patent/CA1248487A/en not_active Expired
- 1984-07-14 DE DE19843426036 patent/DE3426036A1/en active Granted
- 1984-08-01 JP JP59160303A patent/JPS6055082A/en active Pending
- 1984-08-20 GB GB08421098A patent/GB2145426B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6055082A (en) | 1985-03-29 |
| ZA844353B (en) | 1985-02-27 |
| GB2145426A (en) | 1985-03-27 |
| GB8421098D0 (en) | 1984-09-26 |
| DE3426036C2 (en) | 1989-08-03 |
| GB2145426B (en) | 1987-09-16 |
| DE3426036A1 (en) | 1985-03-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4264432A (en) | Pre-heat vaporization system | |
| US4797197A (en) | Delayed coking process | |
| CN102224221B (en) | Conversion of co-fed methane and low hydrogen content hydrocarbon feedstocks to acetylene | |
| EP0036268B1 (en) | Vaporisation and gasification of hydrocarbon feedstocks | |
| KR102366168B1 (en) | Integrated pyrolysis and hydrocracking of crude oil for chemicals | |
| EP0397853B1 (en) | Inhibition of coke formation during vaporization of heavy hydrocarbons | |
| US3870481A (en) | Method for production of synthetic natural gas from crude oil | |
| US7396449B2 (en) | Olefin production utilizing condensate feedstock | |
| US4300998A (en) | Pre-heat vaporization system | |
| US20080283445A1 (en) | Hydrocarbon thermal cracking using atmospheric residuum | |
| US4097363A (en) | Thermal cracking of light gas oil at high severity to ethylene | |
| US20080045613A1 (en) | Process to Prepare Lower Olefins from a Fischer-Tropsch Synthesis Product | |
| US3291573A (en) | Apparatus for cracking hydrocarbons | |
| NL8005758A (en) | PROCESS FOR PREPARING OLEGINS FROM HYDROCARBONS. | |
| KR20080110875A (en) | Improved process for producing lower olefins from heavy hydrocarbon feedstock utilizing two vapor/liquid separators | |
| JPH0421717B2 (en) | ||
| US20010016673A1 (en) | Method of producing olefins and feedstocks for use in olefin production from crude oil having low pentane insolubles and high hydrogen content | |
| CN101583697A (en) | Process for cracking synthetic crude oil-containing feedstock | |
| US1892534A (en) | Process for distillation and conversion of mineral oils | |
| US3855339A (en) | Process for the thermal cracking of hydrocarbons | |
| CA1248487A (en) | Vaporizing heavy hydrocarbon feedstocks without coking | |
| CN103210063B (en) | The technique of crack heavy hydrocarbons charging | |
| KR20040002876A (en) | Process for pyrolyzing a light feed | |
| US5316655A (en) | Process for making light hydrocarbonaceous liquids in a delayed coker | |
| JPS6047097A (en) | Hydrocarbon steam decomposition |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |