CA1204071A - Flexible feed pyrolysis process - Google Patents
Flexible feed pyrolysis processInfo
- Publication number
- CA1204071A CA1204071A CA000461184A CA461184A CA1204071A CA 1204071 A CA1204071 A CA 1204071A CA 000461184 A CA000461184 A CA 000461184A CA 461184 A CA461184 A CA 461184A CA 1204071 A CA1204071 A CA 1204071A
- Authority
- CA
- Canada
- Prior art keywords
- steam
- feed
- heated
- hydrocarbon feed
- temperature
- 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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
Abstract
ABSTRACT OF THE INVENTION
.
Hydrocarbon feed to a steam cracking furnace is heated to near crack-ing temperature by indirect heat exchange with steam to permit use of range of feedstocks.
.
Hydrocarbon feed to a steam cracking furnace is heated to near crack-ing temperature by indirect heat exchange with steam to permit use of range of feedstocks.
Description
Case 0025 F~IBL~ FF.~D PYROLYSIS PROC~S5 _ ,, Th1s ~nvention relatPs to ~team pyrolys~s of hydrocarbons in tubular, fired furnaces to produce cracked gases ronta~ning ethylene.
The basic components of stea~ cracklng or stea~ pyrolys~s furnaces have been unchanged for ~any years. The furnaces co~prise a radlant box Eired to high te~perature with oll or gas and a crackl~g coll disposed w~thin ~he box. Coil outlet temperatures are between abou~ 815C and 930C. The furnaces addi~lonally comprise a convection coll section for utillzat~on of waste heat ln preheating hydrocarbon feed~ heatlng diluent s~eam/ heat~ng the mixed feed of dlluent steam and hydrocarbon feed, and utillty fluid heating for use i~ ehe ethylene unit.
While funda~ental ele~ients of ~hese furnaces are the same, specif~c radiant sectio~ deslgns vary according to require~ents of product mi~, feeds~ock cholce, hea~ eEflclency, and co~t. Nevertheless~ radiant sec-tions can be designed to handle a w~de spectrum of feedstocks and product mixes by varying the dilution ~team ratio aod Eurnace fSring.
Regrett~bly, thls flexlbll~ty does not exlst in the convectlon section because oE the wlde variation in steam and hydrocarbon feed preheat dutie~
that exlst for ethane at one end of the feed spectrum to vacuum gas oil at the oeher end. By way of exa~ple, up to nine time~s as much dllution ~ea~
~ay be required f~r gas oil cracklng than for ethane cracking ~hlch5 in ~urn, requires substant~ally ~arger co~l surface. By way oE further exam~
ple, ~rack~ng conversion to ethy1ene from gas oil l~ substant~ally lower than that fro~ ethaneO For con~tant ethylene production9 therefore~ more gas oll must be preheated and, additlonally9 vaporl~2d. This ~ncreased heat duty, again~ requlres sub~eantially larger coll s~lrf~ceO There are other exa~ples but lt ls sufElclen~ ~o sea~e that si cracking furnace ~Z13~ 7~l ¦ designe~ for ga~ feed~tock cannot be effectively used with a liquid ¦ Ee~dstock and vice versa. To a le~ser exte~t, thls inflexibility alæo ¦ exists between naphtha a~d gas oil feedstDck~.
Aslde from ~he problem of inflex~bll~ty5 1~ should be noted that gas oil feedstocks are notorlously sensitive to preheating because their lncipi-ent cracklng temperature range ls broader and lower than ~hat of lighter Eeedstocks~ In view of the large heat duty requirement for gas oil preheat-ing, relatlvely hot eo~bustion gas in the convect~on seceion is necessarily employed for the heat sourCe. This comblnation of fa~tors often leads to unde~ired cracking in the feed preheat coilO ~ong residence ti~e of feed-6tock in this coil regreteably results in ~ome coke laydown from degenera-tion of the csacking productsO
It is, thereEore, ~n ob~ect of ~his lnventlon to provide a steam cracking process having flexlbility to process a range oE feedstocks. It is a Eurther ob~ect to provide a steam cracking proces~ wh~ch reduces ~he propenslty for coke laydown ~7hen preheating li~d hydrocarbon feedstocks.
According to the invention9 a proce~s is provided for steam crack~ng hydrocarbon feed ~n a tubular~ Eired furnace hav~n~ a radiant section and a convection section whe~ein the hydrocarbon Eeed is heated wi~hin the tem-perature range from abut 370C to about 700C by lndirect heat exchange with ~uperheated steam.
In a prefe~red embodiment of the inventlon~ the steam employed Is superheated in the convection section of the steam cracking furnaceO In a most preferred embodlment~ mixed feed of dilution ~team and hydrocarbon feed ~s heated by lndirect heae exchange wi~h steam that has been su~er-heated ln the onvection sectlon~ When the hydroc~rbon Eeed ~ a gas feed selected fro~ the group consi~tlng of ethane, propane~ and mlxtures there of, the mixed feed 19 heated to a eemperature wlth~n the range from about lZ~34071 600C to aboue 700C. When the hydrocarbon Eeed is naphtha having an endpo~nt between about 150C and about 250C, the ~ixed feed is heated to a te~perature wi~h~n the range from about 430C to about 650C.
When the hydrocarbon feed is gas oil having an endpoint between about 290C and about 570C, the mixed feed ig heated ~o a temperature withln the range from about 450C to about 570C.
F~gure 1 illustra~es a typical prlor are flow sche~e Eor s~eam crack-lng ethane ln which d~lution steam and hyZrocarbon feed preheat~ng duties are furnished by lnd~rect heat exchange with combustion gas ln the convec-tion sectlon of the cracklng furnace, Figure 2 is a flow scheme for stea~ cracklng hydrocarbons by an embodi~
ment of the present inven~ion whereln feed preheating duty and, optionally~
other heat duties are furnished by lndlrect hea~ exchange w~th superheated steam~
Referring first to the prior ar~ configura~ion of Figure 1~ ~here is shown a pyrolysis uni~ compri~ed o~ a tubular fired furnace having a radl-ant section 2 and convectioa BeCtiOn 3. Yer~lcal cracklng ~ubes 4 disposed w~thln the radiant section are heated by ~lo~r burDers 5. Hot combustlon ga~ from the radlant section a~ a cro~sover ~empera~ure of about 11~0C
passes upwardly ~hrough the convection section 3 where heat i~ successi~ely absorbed from the combust~on gas by convectlon coils 6, 7, 8~ 99 10, and 11. The pyrolysis unie addlt~onally co~prises primary que~ch e~changer 12, ~econdary quench exchanger 13~ and stea~ drum 14, The quench exchangers rapidly cool the cracked gases to s~op pyrolysis ~ide reactiolls and recover heat in the fonm of hlgh pressure s~eam.
In operat~on on ethane/propane feedstoc~, proce~s steam recovered from the downstream product separatiODS unit ls utl1ixed as d11ution ~eea~ for the steam cracking process and introduced ~ia line 101 to colls 11 and 9 ~1 ~04~
where lt is heated to about 400C~ The ethanelpropane mi~ture i8 intro-duced ~ia line 102 to co$1 8 where i~ ls prehea~ed to about 430C and then co~bined wi~h hot dlll~tloD steam. The resultlng mlxed f~ed o~ dllu-tlon steam and hydrocarbon feed is ~hen introduced to coil 6 where lt is heated to aboue 650C whlch i8 near ~he inciplent cracking temperature for this feedstock~ The mi~ed feed 1B then introduced to cracklng tubes 4 in the fur~ace radian~ secti~n ~nd the resulting cracked gas is quenched and cooled ln quench e~changers 12 and 13~
Slnce available hea~ ln the convection sectlon i5 ~ore than sufficient ].0 for fec:d preheating, low level hea~ ~s recovered by preheating boiler feed water introduced through llne 103 to coll 10~ Correspondlngly9 high level hea~ i8 recovered from a lo~er portion of the convectlon sectlon by super-heating 315C saturated steam from drum 14 in coll 7~ The re~ul~lng superheated, h~gh pressure stea~ is employed in t~rbine drives in ehe downstream separations section.
The convection coil arrangement of Figure 1 designed for etbane/
propane feed preheating dut~e~ i~ not satisEactory or equlvalent ethylene production from heavier feeds such as naphtha or gas oll. Gas oil, for example, i8 nonmally liquld and ~u~t be fed in subseantially greater quantity than ethane/propane to obt~ln equ~valent ethylene product~onO
Accord~ngly, coil 8 ls too small For complete vaporization of gas oil and llquid carryover to coil 6 will re6ult in coke laydown there~ Furtherg gas oil cracking requires up to ninz ~imes the quantlty of dilution steam required for e~hane/propane cracklng. A3 a re~ult, colls 6, 8, and 9 are underslzed Eor heavy feeds~
Referring now to Flgure 2, an embod~ent Gf the present lnventloll~ the reEerence numerals in com~on with Figure 1 have the same ~dentiflcation and general function except that convection coils 6 and 8 are DOW ln steam ser-vlce in contrast to Flgure 1 where thev were in hydrocarbon heating ser~lce~
iL2-~4V71 F~gure 2 addit~onally sho~s shell and tube heat exchangers 15, 16, 17~
and 18, external to the furnace, w~lch are employed Eor heatlng hydrocarbon feed~tock eo near cracklng ~emperat~re~. Thé figure also ~how~ valves 19 through 27 which~ depend~ng on the par~lcular feedstock characteristics 9 direce feedstock to specif~c sequences of heat e~change ~ccording ~o the requ~red heat~ng dutles.
In operation of the process of the invention as embodied ln Figure 2 using ethane/propane feed~tock, valves 19 through 27 are positioned as ind~-cated in ~he legend on Figure 2. Dilution steam i~ introduced v~a line 201 to coil 8 where ~t is heated tv about 580C and then passPd to heat exchanger 16 where it gives up heat in preheating hyd~ocarbon feed lntro-duced vla llne 202 and coil 10. The feed enter~ng heat exchanger 16 is a~
a temperature of about 245C~ Dilution Rteam and hydrocarbon feed are combined between heat exchangers 16 and 17 and the result~ng ~Ixed feed is further heated to about 650C in heat exchangers 17 and 18 by indirect heat exchange w~th s~esm ~hat has been superheated respectively ln co~ 18 7 .
and 6 in the convection section of the cracking furnace~ The high pressure steam discharged from hea~ exchanger 18 still retains ~ufficlene ~u~erheat for operation of turbine drives in the 3eparatlon~ sect~on cf the olef~ns plantO In the ethane/propane operat~on described, heae e~changer 15 and coil 9 in the furnace conve~tlon bank ~re not in use. A small amount of steam ~ay be passed through coil 9 to prevent excessive ~etal temperatures if necessary.
When operating the process 3ystem oE Figure 2 uslng vacuum gas oil feedstock, ~alves 19 through 27 are repos~tioned as indicaeed ~n ~he legend on Pigure 20 Dilutlon steam introduced through line 201 now pa~ses through coil 9 where it i8 heated to only about 455C and then pa~sed to heat e~changer 15 where it give~ up heae in preheat~ng hydrocarbon fPed intro-duced via line 203. T~e d~lut~on ~team is reheated in coil 8 and passed ~hrough heat e~changer 16 where it gives up hea~ to the mi7~ed feed ILZ0407~L
resulting from the combination of hydrocarbon feed leaving heat exchanger lS and diluti~n stesm leavlng heat exchanger 160 Mi~ed Eeed ls fur~her heaeed to about 540C ln heat e~changers 17 and 18 in the manner prev~-ously described e~eept that operae~ng temperatures ln these heat exchangers S and convection coils 6 and 7 are so~ewha~ lower. A par~icularly unique Eeature of the present lnvention is that gas oll feed rema~ns ~ubstantlally unchanged ~n chemical co~po~ition as ~ passes through the external heat exchangers because of the clo~e temperature control perm~tted by lndirect I heat e~change with steam.
Operation of the process system of Figure 2 on naphtha is not described here other than to no~e that the naphtha ~s also introduced via line 203. This operation i8 readily apparent by reference to the valve legend on Figure 2.
The basic components of stea~ cracklng or stea~ pyrolys~s furnaces have been unchanged for ~any years. The furnaces co~prise a radlant box Eired to high te~perature with oll or gas and a crackl~g coll disposed w~thin ~he box. Coil outlet temperatures are between abou~ 815C and 930C. The furnaces addi~lonally comprise a convection coll section for utillzat~on of waste heat ln preheating hydrocarbon feed~ heatlng diluent s~eam/ heat~ng the mixed feed of dlluent steam and hydrocarbon feed, and utillty fluid heating for use i~ ehe ethylene unit.
While funda~ental ele~ients of ~hese furnaces are the same, specif~c radiant sectio~ deslgns vary according to require~ents of product mi~, feeds~ock cholce, hea~ eEflclency, and co~t. Nevertheless~ radiant sec-tions can be designed to handle a w~de spectrum of feedstocks and product mixes by varying the dilution ~team ratio aod Eurnace fSring.
Regrett~bly, thls flexlbll~ty does not exlst in the convectlon section because oE the wlde variation in steam and hydrocarbon feed preheat dutie~
that exlst for ethane at one end of the feed spectrum to vacuum gas oil at the oeher end. By way of exa~ple, up to nine time~s as much dllution ~ea~
~ay be required f~r gas oil cracklng than for ethane cracking ~hlch5 in ~urn, requires substant~ally ~arger co~l surface. By way oE further exam~
ple, ~rack~ng conversion to ethy1ene from gas oil l~ substant~ally lower than that fro~ ethaneO For con~tant ethylene production9 therefore~ more gas oll must be preheated and, additlonally9 vaporl~2d. This ~ncreased heat duty, again~ requlres sub~eantially larger coll s~lrf~ceO There are other exa~ples but lt ls sufElclen~ ~o sea~e that si cracking furnace ~Z13~ 7~l ¦ designe~ for ga~ feed~tock cannot be effectively used with a liquid ¦ Ee~dstock and vice versa. To a le~ser exte~t, thls inflexibility alæo ¦ exists between naphtha a~d gas oil feedstDck~.
Aslde from ~he problem of inflex~bll~ty5 1~ should be noted that gas oil feedstocks are notorlously sensitive to preheating because their lncipi-ent cracklng temperature range ls broader and lower than ~hat of lighter Eeedstocks~ In view of the large heat duty requirement for gas oil preheat-ing, relatlvely hot eo~bustion gas in the convect~on seceion is necessarily employed for the heat sourCe. This comblnation of fa~tors often leads to unde~ired cracking in the feed preheat coilO ~ong residence ti~e of feed-6tock in this coil regreteably results in ~ome coke laydown from degenera-tion of the csacking productsO
It is, thereEore, ~n ob~ect of ~his lnventlon to provide a steam cracking process having flexlbility to process a range oE feedstocks. It is a Eurther ob~ect to provide a steam cracking proces~ wh~ch reduces ~he propenslty for coke laydown ~7hen preheating li~d hydrocarbon feedstocks.
According to the invention9 a proce~s is provided for steam crack~ng hydrocarbon feed ~n a tubular~ Eired furnace hav~n~ a radiant section and a convection section whe~ein the hydrocarbon Eeed is heated wi~hin the tem-perature range from abut 370C to about 700C by lndirect heat exchange with ~uperheated steam.
In a prefe~red embodiment of the inventlon~ the steam employed Is superheated in the convection section of the steam cracking furnaceO In a most preferred embodlment~ mixed feed of dilution ~team and hydrocarbon feed ~s heated by lndirect heae exchange wi~h steam that has been su~er-heated ln the onvection sectlon~ When the hydroc~rbon Eeed ~ a gas feed selected fro~ the group consi~tlng of ethane, propane~ and mlxtures there of, the mixed feed 19 heated to a eemperature wlth~n the range from about lZ~34071 600C to aboue 700C. When the hydrocarbon Eeed is naphtha having an endpo~nt between about 150C and about 250C, the ~ixed feed is heated to a te~perature wi~h~n the range from about 430C to about 650C.
When the hydrocarbon feed is gas oil having an endpoint between about 290C and about 570C, the mixed feed ig heated ~o a temperature withln the range from about 450C to about 570C.
F~gure 1 illustra~es a typical prlor are flow sche~e Eor s~eam crack-lng ethane ln which d~lution steam and hyZrocarbon feed preheat~ng duties are furnished by lnd~rect heat exchange with combustion gas ln the convec-tion sectlon of the cracklng furnace, Figure 2 is a flow scheme for stea~ cracklng hydrocarbons by an embodi~
ment of the present inven~ion whereln feed preheating duty and, optionally~
other heat duties are furnished by lndlrect hea~ exchange w~th superheated steam~
Referring first to the prior ar~ configura~ion of Figure 1~ ~here is shown a pyrolysis uni~ compri~ed o~ a tubular fired furnace having a radl-ant section 2 and convectioa BeCtiOn 3. Yer~lcal cracklng ~ubes 4 disposed w~thln the radiant section are heated by ~lo~r burDers 5. Hot combustlon ga~ from the radlant section a~ a cro~sover ~empera~ure of about 11~0C
passes upwardly ~hrough the convection section 3 where heat i~ successi~ely absorbed from the combust~on gas by convectlon coils 6, 7, 8~ 99 10, and 11. The pyrolysis unie addlt~onally co~prises primary que~ch e~changer 12, ~econdary quench exchanger 13~ and stea~ drum 14, The quench exchangers rapidly cool the cracked gases to s~op pyrolysis ~ide reactiolls and recover heat in the fonm of hlgh pressure s~eam.
In operat~on on ethane/propane feedstoc~, proce~s steam recovered from the downstream product separatiODS unit ls utl1ixed as d11ution ~eea~ for the steam cracking process and introduced ~ia line 101 to colls 11 and 9 ~1 ~04~
where lt is heated to about 400C~ The ethanelpropane mi~ture i8 intro-duced ~ia line 102 to co$1 8 where i~ ls prehea~ed to about 430C and then co~bined wi~h hot dlll~tloD steam. The resultlng mlxed f~ed o~ dllu-tlon steam and hydrocarbon feed is ~hen introduced to coil 6 where lt is heated to aboue 650C whlch i8 near ~he inciplent cracking temperature for this feedstock~ The mi~ed feed 1B then introduced to cracklng tubes 4 in the fur~ace radian~ secti~n ~nd the resulting cracked gas is quenched and cooled ln quench e~changers 12 and 13~
Slnce available hea~ ln the convection sectlon i5 ~ore than sufficient ].0 for fec:d preheating, low level hea~ ~s recovered by preheating boiler feed water introduced through llne 103 to coll 10~ Correspondlngly9 high level hea~ i8 recovered from a lo~er portion of the convectlon sectlon by super-heating 315C saturated steam from drum 14 in coll 7~ The re~ul~lng superheated, h~gh pressure stea~ is employed in t~rbine drives in ehe downstream separations section.
The convection coil arrangement of Figure 1 designed for etbane/
propane feed preheating dut~e~ i~ not satisEactory or equlvalent ethylene production from heavier feeds such as naphtha or gas oll. Gas oil, for example, i8 nonmally liquld and ~u~t be fed in subseantially greater quantity than ethane/propane to obt~ln equ~valent ethylene product~onO
Accord~ngly, coil 8 ls too small For complete vaporization of gas oil and llquid carryover to coil 6 will re6ult in coke laydown there~ Furtherg gas oil cracking requires up to ninz ~imes the quantlty of dilution steam required for e~hane/propane cracklng. A3 a re~ult, colls 6, 8, and 9 are underslzed Eor heavy feeds~
Referring now to Flgure 2, an embod~ent Gf the present lnventloll~ the reEerence numerals in com~on with Figure 1 have the same ~dentiflcation and general function except that convection coils 6 and 8 are DOW ln steam ser-vlce in contrast to Flgure 1 where thev were in hydrocarbon heating ser~lce~
iL2-~4V71 F~gure 2 addit~onally sho~s shell and tube heat exchangers 15, 16, 17~
and 18, external to the furnace, w~lch are employed Eor heatlng hydrocarbon feed~tock eo near cracklng ~emperat~re~. Thé figure also ~how~ valves 19 through 27 which~ depend~ng on the par~lcular feedstock characteristics 9 direce feedstock to specif~c sequences of heat e~change ~ccording ~o the requ~red heat~ng dutles.
In operation of the process of the invention as embodied ln Figure 2 using ethane/propane feed~tock, valves 19 through 27 are positioned as ind~-cated in ~he legend on Figure 2. Dilution steam i~ introduced v~a line 201 to coil 8 where ~t is heated tv about 580C and then passPd to heat exchanger 16 where it gives up heat in preheating hyd~ocarbon feed lntro-duced vla llne 202 and coil 10. The feed enter~ng heat exchanger 16 is a~
a temperature of about 245C~ Dilution Rteam and hydrocarbon feed are combined between heat exchangers 16 and 17 and the result~ng ~Ixed feed is further heated to about 650C in heat exchangers 17 and 18 by indirect heat exchange w~th s~esm ~hat has been superheated respectively ln co~ 18 7 .
and 6 in the convection section of the cracking furnace~ The high pressure steam discharged from hea~ exchanger 18 still retains ~ufficlene ~u~erheat for operation of turbine drives in the 3eparatlon~ sect~on cf the olef~ns plantO In the ethane/propane operat~on described, heae e~changer 15 and coil 9 in the furnace conve~tlon bank ~re not in use. A small amount of steam ~ay be passed through coil 9 to prevent excessive ~etal temperatures if necessary.
When operating the process 3ystem oE Figure 2 uslng vacuum gas oil feedstock, ~alves 19 through 27 are repos~tioned as indicaeed ~n ~he legend on Pigure 20 Dilutlon steam introduced through line 201 now pa~ses through coil 9 where it i8 heated to only about 455C and then pa~sed to heat e~changer 15 where it give~ up heae in preheat~ng hydrocarbon fPed intro-duced via line 203. T~e d~lut~on ~team is reheated in coil 8 and passed ~hrough heat e~changer 16 where it gives up hea~ to the mi7~ed feed ILZ0407~L
resulting from the combination of hydrocarbon feed leaving heat exchanger lS and diluti~n stesm leavlng heat exchanger 160 Mi~ed Eeed ls fur~her heaeed to about 540C ln heat e~changers 17 and 18 in the manner prev~-ously described e~eept that operae~ng temperatures ln these heat exchangers S and convection coils 6 and 7 are so~ewha~ lower. A par~icularly unique Eeature of the present lnvention is that gas oll feed rema~ns ~ubstantlally unchanged ~n chemical co~po~ition as ~ passes through the external heat exchangers because of the clo~e temperature control perm~tted by lndirect I heat e~change with steam.
Operation of the process system of Figure 2 on naphtha is not described here other than to no~e that the naphtha ~s also introduced via line 203. This operation i8 readily apparent by reference to the valve legend on Figure 2.
Claims (6)
1. In a process for steam cracking hydrocarbon feed in a tubular, fired furnace having a radiant section and a convection section wherein dilution steam is added to the hydrocarbon feed and the resulting mixed feed of dilution steam and hydrocarbon feed is heated to near incipient cracking temperature prior to introduction of the mixed feed to the radiant section, the improvement which comprises heating the hydrocarbon feed with-in the temperature range from about 370°C to about 700°C by indirect heat exchange with superheated steam.
2. The process of claim 1 wherein at least a portion of the super-heated steam is superheated in the convection section.
3. The process of either claim 1 or claim 2 wherein the hydrocarbon feed is selected from the group consisting of ethane, propane, or mixtures thereof and the mixed feed is heated by indirect heat exchange with super-heated steam to a temperature within the range from about 600°C to about 700°C.
4. The process of either claim 1 or claim 2 wherein the hydrocarbon feed is naphtha having an end point between about 150°C and about 250°C
and the mixed feed is heated by indirect heat exchange with superheated steam to a temperature within the range from about 430°C to about 650°C.
and the mixed feed is heated by indirect heat exchange with superheated steam to a temperature within the range from about 430°C to about 650°C.
5. The process of either claim 1 or claim 2 wherein the hydrocarbon feed is gas oil having an end point between about 290°C and about 570°C
and the mixed feed is heated by indirect heat exchange with superheated steam to a temperature within the range from about 450°C to about 570°C.
and the mixed feed is heated by indirect heat exchange with superheated steam to a temperature within the range from about 450°C to about 570°C.
6. The process of claim 2 wherein the process for steam cracking additionally comprises a cracked gas quench boiler for raising at least a portion of the steam that is superheated in the convection section
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US561,408 | 1983-12-14 | ||
| US06/561,408 US4479869A (en) | 1983-12-14 | 1983-12-14 | Flexible feed pyrolysis process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1204071A true CA1204071A (en) | 1986-05-06 |
Family
ID=24241844
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000461184A Expired CA1204071A (en) | 1983-12-14 | 1984-08-16 | Flexible feed pyrolysis process |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US4479869A (en) |
| EP (1) | EP0146117B1 (en) |
| JP (1) | JPS60130679A (en) |
| KR (1) | KR910008564B1 (en) |
| CA (1) | CA1204071A (en) |
| DE (1) | DE3481315D1 (en) |
Families Citing this family (38)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4552644A (en) * | 1982-09-30 | 1985-11-12 | Stone & Webster Engineering Corporation | Duocracking process for the production of olefins from both heavy and light hydrocarbons |
| JPS601138A (en) * | 1983-06-17 | 1985-01-07 | Mitsubishi Heavy Ind Ltd | Thermal cracking process for selective production of olefin and aromatic hydrocarbon from hydrocarbon |
| US4615795A (en) * | 1984-10-09 | 1986-10-07 | Stone & Webster Engineering Corporation | Integrated heavy oil pyrolysis process |
| US4617109A (en) * | 1985-12-23 | 1986-10-14 | The M. W. Kellogg Company | Combustion air preheating |
| US4908121A (en) * | 1986-05-12 | 1990-03-13 | The M. W. Kellogg Company | Flexible feed pyrolysis process |
| US4822940A (en) * | 1987-08-17 | 1989-04-18 | The Standard Oil Company | Process for converting light hydrocarbons and/or natural gas to liquid hydrocarbons |
| US4929789A (en) * | 1988-01-15 | 1990-05-29 | The Standard Oil Company | Process for pyrolyzing or thermal cracking a gaseous or vaporized hydrocarbon feedstock using a novel gas-solids contacting device and an oxidation catalyst |
| US5190634A (en) * | 1988-12-02 | 1993-03-02 | Lummus Crest Inc. | Inhibition of coke formation during vaporization of heavy hydrocarbons |
| US5120892A (en) * | 1989-12-22 | 1992-06-09 | Phillips Petroleum Company | Method and apparatus for pyrolytically cracking hydrocarbons |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US3124424A (en) * | 1964-03-10 | high temperature thermal cracking | ||
| US2111899A (en) * | 1935-12-18 | 1938-03-22 | Nagel Theodore | Process for the manufacture of ethylene from oil |
| US2111900A (en) * | 1936-02-08 | 1938-03-22 | Nagel Theodore | Process for the manufacture of ethylene from oil |
| US2176962A (en) * | 1938-04-28 | 1939-10-24 | Theodore Nagel | Process for producing ethylene from oil |
| US2945076A (en) * | 1957-04-15 | 1960-07-12 | Gulf Research Development Co | Process for producing olefins |
| NL6802193A (en) * | 1967-02-23 | 1968-08-26 | ||
| SU633892A1 (en) * | 1972-05-30 | 1978-11-25 | Предприятие П/Я Р-6830 | Device for retreatment of hydrocarbon raw stock |
| US4107226A (en) * | 1977-10-19 | 1978-08-15 | Pullman Incorporated | Method for quenching cracked gases |
| DE2854061A1 (en) * | 1978-12-14 | 1980-07-03 | Linde Ag | METHOD FOR PREHEATING HYDROCARBONS BEFORE THERMAL CLEAVING |
| US4324649A (en) * | 1980-07-08 | 1982-04-13 | Pullman Incorporated | Fired process heater |
| US4321131A (en) * | 1981-04-15 | 1982-03-23 | Union Carbide Corporation | Process for heat carrier generation |
-
1983
- 1983-12-14 US US06/561,408 patent/US4479869A/en not_active Expired - Lifetime
-
1984
- 1984-08-16 CA CA000461184A patent/CA1204071A/en not_active Expired
- 1984-09-27 JP JP59202897A patent/JPS60130679A/en active Granted
- 1984-10-20 KR KR1019840006535A patent/KR910008564B1/en not_active IP Right Cessation
- 1984-12-12 DE DE8484115302T patent/DE3481315D1/en not_active Expired - Lifetime
- 1984-12-12 EP EP84115302A patent/EP0146117B1/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| EP0146117A2 (en) | 1985-06-26 |
| DE3481315D1 (en) | 1990-03-15 |
| KR850004980A (en) | 1985-08-19 |
| EP0146117A3 (en) | 1987-07-15 |
| US4479869A (en) | 1984-10-30 |
| JPS60130679A (en) | 1985-07-12 |
| KR910008564B1 (en) | 1991-10-19 |
| EP0146117B1 (en) | 1990-02-07 |
| JPH0546398B2 (en) | 1993-07-13 |
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