WO2022268706A1 - Olefins production process - Google Patents
Olefins production process Download PDFInfo
- Publication number
- WO2022268706A1 WO2022268706A1 PCT/EP2022/066711 EP2022066711W WO2022268706A1 WO 2022268706 A1 WO2022268706 A1 WO 2022268706A1 EP 2022066711 W EP2022066711 W EP 2022066711W WO 2022268706 A1 WO2022268706 A1 WO 2022268706A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- stream
- feed stream
- steam
- heated
- cracker furnace
- Prior art date
Links
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 title description 12
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 73
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 73
- 238000010438 heat treatment Methods 0.000 claims abstract description 62
- 239000002737 fuel gas Substances 0.000 claims abstract description 57
- 238000000034 method Methods 0.000 claims abstract description 51
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000001301 oxygen Substances 0.000 claims abstract description 47
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 47
- 238000005336 cracking Methods 0.000 claims abstract description 34
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 47
- 239000003546 flue gas Substances 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 41
- 229910001868 water Inorganic materials 0.000 claims description 41
- 239000001257 hydrogen Substances 0.000 description 25
- 229910052739 hydrogen Inorganic materials 0.000 description 25
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 24
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 24
- 239000004215 Carbon black (E152) Substances 0.000 description 20
- 229910052799 carbon Inorganic materials 0.000 description 17
- 238000010790 dilution Methods 0.000 description 16
- 239000012895 dilution Substances 0.000 description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 14
- 239000001569 carbon dioxide Substances 0.000 description 12
- 229910002092 carbon dioxide Inorganic materials 0.000 description 12
- 239000007789 gas Substances 0.000 description 8
- 229930195734 saturated hydrocarbon Natural products 0.000 description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 238000010626 work up procedure Methods 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 239000003915 liquefied petroleum gas Substances 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 101100294139 Caenorhabditis elegans aph-2 gene Proteins 0.000 description 3
- 101150089041 aph-1 gene Proteins 0.000 description 3
- 239000001273 butane Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000003085 diluting agent Substances 0.000 description 3
- -1 ethylene, propylene, butylenes Chemical class 0.000 description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 238000004230 steam cracking Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000001991 steam methane reforming Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- 229910001018 Cast iron Inorganic materials 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/002—Cooling of cracked gases
Definitions
- the present invention relates to a process for producing olefins from a feed stream containing hydrocarbons, by pyrolytic cracking of the hydrocarbons in a cracker furnace.
- Pyrolytic cracking of hydrocarbons in a cracker furnace is a petrochemical process that is widely used to produce olefins (such as ethylene, propylene, butylenes and butadiene) and optionally aromatics (such as benzene, toluene and xylene). Where such pyrolytic cracking is performed in the presence of dilution steam, this is referred to as "steam cracking".
- the feed stream to such pyrolytic cracking process may include one or more of ethane, propane, butane, liquefied petroleum gas (LPG), naphtha, hydrowax and recycled waste plastics oil.
- LPG liquefied petroleum gas
- the hydrocarbons containing stream is converted under the influence of heat, and substantially in the absence of oxygen, into an olefins containing effluent.
- a cracker furnace comprises a convection section and a radiant section.
- the convection section When considering the direction of the feed stream through a cracker furnace, the convection section is located in an upstream part of the cracker furnace and the radiant section is located in a downstream part thereof.
- the convection section when considering the direction of the below- mentioned flue gas through a cracker furnace, the convection section is located in a downstream part of the cracker furnace and the radiant section is located in an upstream part thereof.
- the convection section comprises one or more tubes into which the hydrocarbon feed stream is introduced, in which tubes the hydrocarbon stream is pre-heated by hot flue gas which is present outside these tubes and which arises from the radiant section, wherein heat exchange takes place through the walls of said tubes.
- Said radiant section comprises one or more burners wherein oxygen, e.g. as present in air, and a fuel gas are contacted and the fuel gas is combusted resulting in heat release, which heat is needed to effect the pyrolytic cracking of the hydrocarbon stream in one or more tubes which are also comprised within the radiant section and into which the pre-heated hydrocarbon stream from the convection section is introduced.
- the fuel gas used in said burners comprises hydrogen and methane originating from the olefins containing effluent from the radiant section of the cracker furnace.
- CCS Carbon Capture and Storage
- CCU Carbon Capture and Use
- the present invention to reduce the total amount of fuel gas needed to produce the desired olefins as contained in the olefins containing effluent from the cracker furnace.
- An important advantage of such reduced fuel gas consumption is that the amount of carbon dioxide formed in the burners of the cracker furnace relative to the amount of desired products (i.e. olefins and optionally aromatics) is decreased.
- the fuel gas comprises hydrogen which originates from another source than the cracker furnace effluent (e.g.
- the above-mentioned reduced fuel gas consumption advantageously results in that less of such on-purpose hydrogen may be needed as cracker furnace fuel gas so that accordingly less hydrogen production may be needed which production may also involve the formation of carbon dioxide and/or may require the use of renewable, non-fossil energy resources which may be limited available.
- Such technically advantageous process would preferably result in a relatively low energy demand and/or relatively low capital expenditure.
- one or more of the above- mentioned objectives may be achieved by both (i) pre-heating the hydrocarbon feed stream, that is fed to the convection section of a cracker furnace, outside that cracker furnace, and (ii) pre-heating the oxygen containing stream that is fed to a burner in the radiant section of the cracker furnace and contacted therein with a fuel gas, whereby said burner advantageously needs to provide a reduced heat duty for performing the pyrolytic cracking process at the same pyrolytic cracking process product output.
- a reduced heat duty relative to the amount of desired products (i.e. olefins and optionally aromatics) in the effluent from the cracker furnace is achieved.
- less fuel gas needs to be combusted in said burner and accordingly, in case the fuel gas comprises e.g. methane, less carbon dioxide is formed and ends up in the flue gas resulting from that combustion.
- the so-called stack temperature of the flue gas that is emitted into the Earth's atmosphere after having heated the hydrocarbon feed in the radiant and convection sections of the cracker furnace, surprisingly, can still be maintained relatively low, despite the higher inlet temperature of the pre-heated hydrocarbon feed introduced into the convection section in accordance with the present invention, thereby requiring less heat input from the flue gas present in that same convection section.
- the same, relatively low stack temperature of the flue gas may still be achieved in the present invention, even at the relatively high inlet temperature of the hydrocarbon feed. Keeping the stack temperature the same is important for ensuring that the overall thermal efficiency of the cracker furnace is not decreased.
- the present invention relates to a process for producing olefins from a feed stream containing hydrocarbons by pyrolytic cracking of the hydrocarbons in a cracker furnace, said process comprising: pre-heating the feed stream outside the cracker furnace; feeding the pre-heated feed stream to a tube in the convection section of the cracker furnace; further pre-heating the feed stream in the convection section; feeding the further pre-heated feed stream to a tube in the radiant section of the cracker furnace; pre-heating an oxygen containing stream; contacting the pre-heated oxygen containing stream with a fuel gas in a burner in the radiant section; and pyrolytic cracking the feed stream in the radiant section resulting in an effluent containing olefins.
- Figure 1 shows a set-up for the below Reference Example (not according to the present invention), as applied in a process for producing olefins from a feed stream containing hydrocarbons by pyrolytic cracking of the hydrocarbons in a cracker furnace.
- Figure 2 shows an alternative set-up for below Example A (according to the present invention), for such olefins production process.
- the process of the present invention comprises multiple steps.
- said process may comprise one or more intermediate steps between consecutive steps.
- said process may comprise one or more additional steps preceding the first step and/or following the last step.
- said process may comprise one or more intermediate steps between steps a) and b) and between steps b) and c).
- said process may comprise one or more additional steps preceding step a) and/or following step c).
- a stream or a composition comprises two or more components
- these components are to be selected in an overall amount not to exceed 100%.
- the present invention concerns a process for producing olefins from a feed stream containing hydrocarbons by pyrolytic cracking of the hydrocarbons in a cracker furnace.
- the above-mentioned cracker furnace comprises a convection section and a radiant section.
- the convection section is located in an upstream part of the cracker furnace and the radiant section is located in a downstream part thereof.
- the present process comprises a number of steps.
- Said process comprises pre-heating the feed stream containing hydrocarbons outside the cracker furnace, feeding the pre heated feed stream to a tube in the convection section, further pre-heating the feed stream in the convection section, feeding the further pre-heated feed stream to a tube in the radiant section, pyrolytic cracking the feed stream in the radiant section resulting in an effluent containing olefins and optionally aromatics).
- pre-heating refers to heating a stream before introducing such stream into the radiant section of the cracker furnace.
- the feed stream containing hydrocarbons may be pre-heated in the convection section of the cracker furnace before pre-heating the feed stream outside the cracker furnace.
- pre-heating the feed stream containing hydrocarbons outside the cracker furnace is performed before feeding the feed stream to a tube in the convection section of the cracker furnace for a first time.
- the feed stream containing hydrocarbons is not pre-heated in the convection section of the cracker furnace before pre-heating the feed stream outside the cracker furnace.
- pre-heating through indirect heat exchange does not involve direct contact between the heating medium and the medium to be heated.
- pre-heating through indirect heat exchange may involve the use of an intermediate fluid as a heat transfer medium.
- said intermediate fluid does not comprise steam.
- pre-heating through indirect heat exchange may not involve the use of an intermediate fluid.
- a “tube in the convection section” refers to a tube suitable for carrying a flow of fluid, such as a gas or a liquid, in which tube the feed stream containing hydrocarbons is further pre-heated.
- a "tube in the radiant section” refers to a tube suitable for carrying a flow of a gas, in which tube the further pre-heated feed stream containing hydrocarbons is pyrolytically cracked.
- pre-heating of the hydrocarbon feed before feeding into the radiant section of the cracker furnace does not only take place in the convection section of the cracker furnace but also outside that cracker furnace.
- Said pre-heating inside the cracker furnace takes place through indirect heat exchange with the flue gas coming from the radiant section, i.e. a heat transfer from the hot flue gas present in the convection section outside a tube in that same convection section to the hydrocarbon feed stream as fed into said tube.
- the feed stream containing hydrocarbons may be pre-heated to any temperature, preferably to a temperature which is higher than ambient temperature.
- said feed stream is pre-heated outside the cracker furnace to a temperature of at most 550 °C, more preferably at most 500 °C, more preferably at most 450 °C, more preferably at most 400 °C, most preferably at most 350 °C.
- said feed stream is pre-heated outside the cracker furnace to a temperature of at least 75 °C, more preferably at least 100 °C, more preferably at least 150 °C, more preferably at least 200 °C, more preferably at least 250 °C, most preferably at least 300 °C.
- the feed stream that is pre-heated outside the cracker furnace is fed to a tube in the convection section and further pre-heated therein, preferably to a temperature of from 300 to 800 °C, more preferably of from 500 to 700 °C, most preferably of from 550 to 650 °C.
- the further pre-heated feed stream from the convection section is fed to a tube in the radiant section, wherein pyrolytic cracking of hydrocarbons in the feed stream is performed, preferably at a temperature of from 700 to 1000 °C, more preferably 700 to 950 °C, most preferably 700 to 900 °C, resulting in an effluent containing olefins.
- the heat duty required for enabling pyrolytic cracking of the hydrocarbons in one or more tubes in the radiant section is delivered by one or more burners in the radiant section, wherein oxygen and a fuel gas are contacted and the fuel gas is combusted resulting in heat release in the form of a hot flue gas, further resulting in an indirect heat exchange, i.e. a heat transfer from the hot flue gas present in the radiation section outside a tube in that same radiation section to the further pre-heated hydrocarbon feed stream as fed into said tube.
- the olefins-containing effluent leaving the radiant section is still hot and may be used, in the present invention, to provide steam having a relatively high pressure and a relatively high temperature through indirect heat exchange, using so-called "Transfer Line Exchangers" (TLEs), before the effluent is fed to a work-up section outside the cracker furnace in which work-up section several products are separated from the effluent.
- TLEs Transfer Line Exchangers
- Said (TLEs) are used to rapidly cool the effluent from a cracker furnace, which TLEs are further discussed below.
- Such pressurized steam may be generated from water, which may also be referred to as "boiler feed water” (BFW) or “utility water” as opposed to “process water” which process water may be added in the form of steam as a diluent to the hydrocarbon feed itself.
- BFW battery feed water
- utility water or BFW
- heat for generating said high temperature pressurized steam may be obtained by indirect heat exchange with the olefins containing effluent (“process effluent”) from the radiant section, but also by indirect heat exchange with the flue gas in one or more of so-called "banks" in the convection section.
- VHP very high pressure
- HP high pressure
- MP medium pressure
- LP low pressure
- Such types of pressurized steam may be superheated, where the surplus superheat temperature above the steam saturation temperature may be at least 10 °C or at least 20 °C or at least 30 °C. Further, said surplus superheat temperature may be at most 250 °C or at most 200 °C or at most 100 °C.
- one or more of the above- mentioned pressurized steam types and another heat source having a temperature of from greater than 50 °C to 100 °C or of from greater than 50 °C to 90 °C, which said other heat source may have an atmospheric pressure (e.g. process or utility water, or hydrocarbon streams run down from a cracker unit, or hydrocarbon streams within a cracker unit), may be used in pre-heating the feed stream containing hydrocarbons outside the cracker furnace through indirect heat exchange between the feed stream and such steam or other heat source.
- Said other lower temperature heat source (not including pressurized steam) may comprise waste heat that is available in a plant for the production of olefins involving cracking of hydrocarbons.
- Said pre-heating of the feed stream containing hydrocarbons outside the cracker furnace may be carried out in one step or two or more steps, wherein the temperature of the heat source in a preceding pre-heating step is lower than the temperature of the heat source in a subsequent pre-heating step.
- said steam may be generated by heat recovered from the cracker furnace, for example from the olefins containing effluent from the radiant section and/or from flue gas in the convection section.
- steam that may be used in such indirect heat exchange may have a pressure of from greater than atmospheric pressure to 130 bara and a temperature of from greater than 100 °C to 570 °C.
- one or more of above-mentioned LP steam, MP steam and HP steam is or are used for such pre heating.
- two or more different steam types are used for such pre-heating in different subsequent steps, in the 1 st step the lowest pressure steam is used and in the last step the highest pressure steam is used.
- At least a portion of the olefins containing effluent from the radiant section may be used in a direct sense in pre-heating the feed stream containing hydrocarbons outside the cracker furnace through indirect heat exchange between the feed stream and said effluent. This is different from first generating steam using said effluent as heat source and then using the generated steam as a heat source in the feed pre-heating step, as discussed above. Further, in the present invention, in addition to pre heating the feed stream containing hydrocarbons outside the cracker furnace, any dilution steam may also be pre-heated outside the cracker furnace separately from pre-heating said feed stream.
- steam cracking As mentioned above, where pyrolytic cracking of hydrocarbons in a cracker furnace is performed in the presence of dilution steam, this is referred to as “steam cracking". Further, said dilution steam is "process water" which, as opposed to “utility water”, is added in the form of steam as a diluent to the hydrocarbon feed itself. In a case wherein dilution steam is pre-heated outside the cracker furnace, such pre-heating may be performed in the same way as described above with respect to pre-heating the feed stream.
- such pre-heating of dilution steam outside the cracker furnace may be carried out by an indirect heat exchange with one or more of the above-mentioned heat sources for pre-heating the feed stream containing hydrocarbons, such heat sources including "VHP”, “HP”, “MP” and "LP” steam.
- an oxygen containing stream is contacted with a fuel gas in a burner in the radiant section, which stream is first pre-heated before such contacting takes place.
- the latter pre-heating may be carried out inside or outside the cracker furnace, preferably inside the cracker furnace, in particular in the convection section thereof.
- Pre-heating of the oxygen containing stream outside the cracker furnace may be carried out by an indirect heat exchange with one or more of the above-mentioned heat sources for pre-heating the feed stream containing hydrocarbons, such heat sources including "VHP", "HP", "MP” and "LP" steam.
- heat sources including "VHP", "HP", "MP” and "LP” steam.
- a suitable example of pre-heating the oxygen containing stream outside the cracker furnace is a case wherein the above- described LP steam is used as a heat source for such pre- heating, especially in a case where there is a surplus of LP steam after having pre-heated the feed stream containing hydrocarbons outside the cracker furnace as described above.
- Pre-heating the oxygen containing stream outside the cracker furnace advantageously results in reduced fuel gas consumption.
- suitable heat sources for such pre heating comprise: LP steam, warm water (e.g. as available after heat exchange in quench water tower for dilution steam condensation) having a temperature of from 60 to 90 °C and low-pressure condensate having a temperature of from 100 to 200 °C.
- Said oxygen containing stream which is contacted with the fuel gas may comprise an air stream. Alternatively or additionally, it may comprise a stream containing more or less oxygen than air. In particular, such stream containing more or less oxygen than air may be combined with an air stream, before contacting with the fuel gas.
- a suitable example of a stream which may contain less oxygen than air is below-mentioned exhaust gas stream from a gas turbine used for power generation (e.g. electrical or shaft power). Such exhaust gas stream may contain oxygen in an amount of from 12 to 18 vol.%, typically around 15 vol.%.
- the oxygen containing stream which is contacted with the fuel gas may contain oxygen in an amount greater than 10 vol.% or greater than 12 vol.% or greater than 21 vol.%. Further, said stream may contain at most 99.9 vol.% of oxygen.
- the above-mentioned oxygen containing stream which is contacted with the fuel gas may be pre-heated to a temperature of from 70 to 550 °C. Said temperature may be at least 70 °C or at least 100 °C or at least 150 °C. Further, said temperature may be at most 550 °C or at most 450 °C or at most 400 °C or at most 350 °C.
- the oxygen containing stream which is contacted with the fuel gas may be pre-heated through indirect heat exchange between the oxygen containing stream and flue gas in the convection section.
- Heat exchange device equipment to enable this may for example comprise a LCAP ("Liquid Coupled Air Preheater") in which an intermediate fluid is used as heat transfer medium.
- the flue gas heat is reduced before this would be emitted as a loss to the atmosphere, and is indirectly transferred as useful heat duty to combustion oxygen resulting in a reduction of fuel gas consumption.
- the heat exchange device equipment may comprise a single equipment heat exchanger, e.g. a "plates and frame” type heat exchanger, or a tubular heat exchanger, or a combination thereof, and with or without fins applied to either such plates or tubes.
- a single equipment heat exchanger e.g. a "plates and frame” type heat exchanger, or a tubular heat exchanger, or a combination thereof, and with or without fins applied to either such plates or tubes.
- An example of such "plates and frame” type heat exchanger is a recuperative static heat exchanger equipment whereby heat is transferred through a surface made of rectangular, finned channels. These channels are stacked vertically alongside each other to form rows, then the various horizontal rows on top of each other form a single module.
- modules are stacked on top of each other to create a multi-pass arrangement.
- the flue gas passes vertically downward outside over the channels, while the oxygen containing supply flows in a cross-counter flow into and inside the channels.
- An example of such "plates and frame” type heat exchanger is a cast-iron "DEKA” heat exchanger which is commercially available.
- the heat exchange device equipment may be of a regenerative type.
- An example of the latter heat exchange device equipment is a commercially available Ljungstrom ® heat exchanger which comprises a shaft connected to a rotor with heat transfer plates.
- the oxygen containing stream which is contacted with the fuel gas may be pre-heated through direct heat exchange between the oxygen containing stream and flue gas from the convection section by mixing these outside the cracker furnace prior to introduction into (a burner in) the radiant section.
- the above-described indirect and direct heat exchange between convection section flue gas and an oxygen containing stream are both technically feasible and the selection choice may depend on furnace design geometry, available plot space and utility connection locations, which may be optimized during detailed design.
- an oxygen containing stream which may have been pre-heated, may be mixed with another oxygen containing stream having a different temperature, before contacting with the fuel gas.
- Said other oxygen containing stream may have a higher temperature, such as an exhaust gas stream from a gas turbine used for power generation which stream may still contain around 15 vol.% of oxygen as further described above.
- said other oxygen containing stream may have a lower temperature, thereby reducing the temperature of the combined oxygen containing stream to be contacted with the fuel gas.
- Such other oxygen containing stream having a lower temperature is preferably an oxygen-enriched stream containing oxygen in an amount greater than 21 vol.%.
- the pre-heated oxygen containing stream is then contacted with the fuel gas in a burner in the radiant section.
- Said fuel gas may comprise hydrogen and methane, in specific hydrogen and methane originating from the olefins containing effluent from the radiant section of the cracker furnace.
- hydrogen may be used as the only fuel gas.
- said fuel gas may comprise at most 99.9 vol.% of hydrogen.
- the fuel gas may comprise hydrogen originating from the above-mentioned olefins containing effluent and/or hydrogen that is generated elsewhere.
- the present invention does result in lowering the demand of such hydrogen fuel which would be sourced from relatively expensive on-purpose generation through renewable power electrolysis (so-called “green” hydrogen), or steam methane reforming in combination with Carbon Capture and Use (CCU) or Carbon Capture and Sequestration (CCS) (so-called “blue” hydrogen), or other forms of hydrogen produced external to the cracker furnace which production may involve the formation of carbon dioxide and which hydrogen may be relatively expensive.
- renewable power electrolysis so-called “green” hydrogen
- CCU Carbon Capture and Use
- CCS Carbon Capture and Sequestration
- the reduced fuel gas consumption advantageously results in that less of such hydrogen may be needed so that accordingly less external hydrogen production may be needed which production may also involve the formation of carbon dioxide and/or may require the use of renewable, non-fossil energy resources which may be limited available (and hence relatively expensive) .
- An additional advantage of pre-heating the feed stream containing hydrocarbons outside the cracker furnace, in accordance with the present invention, is that heat exchangers outside the furnace are easier to clean than the convection section banks within the furnace itself.
- heat exchangers can be placed in parallel which allows for some fouling to take place because one of the heat exchangers may be taken out of service for cleaning.
- Such parallel placement of convection section banks within the furnace itself is usually not possible or complicated.
- pre heating in the convection section of the cracker one needs to be stringent on hydrocarbon feed related fouling risk. In the present invention, said risk is less important.
- Yet another advantage of the present invention is that it allows a cracker furnace design which can be applied generically to a wider variation of hydrocarbon feedstocks ranging from ethane to heavy liquid feeds, as compared to conventional cracker furnaces of which its design may be feed-specific to ethane, propane, butane, mixed LPG, naphtha, condensate or a heavier liquid feed.
- pre heating which may also include vaporization, of the feed stream containing hydrocarbons outside the cracker furnace, as in the present invention, that furnace may be designed in a more generic way accommodating different types of hydrocarbon feedstocks.
- the stream that is fed to the present process for producing olefins is a stream containing hydrocarbons.
- Said feed stream contains saturated hydrocarbons. In addition, it may contain unsaturated hydrocarbons. Further, before said feed stream is subjected to the present process, it may be gaseous or may be in liquid form.
- said feed stream may comprise one or more of ethane, propane, butane, liquefied petroleum gas (LPG), naphtha, hydrowax and recycled waste plastics oil.
- LPG liquefied petroleum gas
- the cracking may be performed in any known way.
- the cracking is performed at an elevated temperature, preferably in the range of from 650 to 1000 °C, more preferably of from 700 to 900 °C, most preferably of from 750 to 850 °C.
- Steam is usually added to the cracking zone (which is also referred to as "steam cracking"), acting as a diluent to reduce the hydrocarbon partial pressure and thereby enhance the olefin yield. Steam also reduces the formation and deposition of carbonaceous material or coke in the cracking zone.
- the cracking occurs in the absence of oxygen.
- the residence time at the cracking conditions is very short, suitably of from 0.05 to 0.8 second, more suitably of from 0.10 to 0.6 second.
- a cracker effluent is obtained that may comprise aromatics (as produced in the cracking process) which may include one or more of benzene, toluene and xylene, and that comprises olefins which may include one or more of ethylene, propylene, butylenes and butadiene, and hydrogen, water and carbon dioxide.
- aromatics as produced in the cracking process
- olefins which may include one or more of ethylene, propylene, butylenes and butadiene
- hydrogen, water and carbon dioxide hydrogen, water and carbon dioxide.
- the specific products obtained depend on the composition of the feed, the hydrocarbon-to- steam ratio, the cracking temperature and the furnace residence time.
- the cracked products from the cracker are then passed through a system comprising one or more indirect heat exchangers, such system often referred to as a TLE ("transfer line exchanger").
- a TLE comprises multiple heat exchangers, they can be arranged in parallel and/or in series. Further, if multiple TLEs are used, they can be arranged in parallel and/or in series, preferably in series.
- the temperature of the cracked products is reduced. In this way, the composition of the process gas may be rapidly frozen.
- the TLEs preferably cool the cracked products by reducing the temperature at the outlet of the TLE or the final TLE to a temperature in the range of from 150 to 700 °C.
- the above-mentioned cooling of the cracker process effluent in a TLE, downstream of the outlet of the cracker furnace, may be carried out in two or more stages, using two or more TLEs arranged in series.
- pressurized steam is generated from water, which may also be referred to as "boiler feed water” (BFW) or "utility water” as mentioned above, by indirect exchange with the cracker effluent in a first TLE.
- BFW water feed water
- the first TLE reduces the effluent temperature to a higher temperature which may be at least 220 °C or at least 260 °C and which may be at most 700 °C or at most 650 °C.
- a first TLE in another embodiment wherein two or more TLEs arranged in series are used, in a first TLE at least a portion of the feed stream containing hydrocarbons is pre heated and in the next TLE pressurized steam is generated from water (i.e. from utility or boiler feed water), that is to say in the reversed order as in the above-mentioned preferred embodiment.
- the steam generated in the second TLE may be saturated or unsaturated steam.
- WO2018229267 and US4479869 describe the use of secondary TLEs in conventional steam crackers.
- above-mentioned utility water may also be pre-heated outside the cracker furnace before pressurized steam is generated therefrom as described above.
- Such pre heating of utility water may be carried out by an indirect heat exchange with one or more of the above-mentioned heat sources for pre-heating the feed stream containing hydrocarbons, such heat sources including "VHP", "HP", "MP” and "LP” steam.
- the pre-heated utility water may then be sent to a bank in the convection section of the cracker furnace, in which bank (often referred to as an "economiser” bank) an indirect heat exchange with the flue gas originating from the radiant section takes place.
- bank often referred to as an "economiser” bank
- the water fed to said "economiser” bank since the water fed to said "economiser” bank has already been pre-heated, less heat is extracted from flue gas in the convection section, resulting more heat further available to pre-heat combustion air and a further reduced fuel gas consumption.
- the further heated water resulting from above-mentioned "economiser” bank may then be sent to a steam drum outside the cracker furnace and then to a TLE wherein indirect heat exchange with process effluent from the radiant section of the cracker furnace takes place.
- the resulting steam may then be sent to another bank in the convection section of the cracker furnace, which is positioned below the above- mentioned "economiser” bank, in which other bank (often referred to as a "steam superheat” or "SSH" bank) an indirect heat exchange with the flue gas originating from the radiant section takes place, which may result in superheated steam wherein substantially all of the water is in gaseous form.
- SSH steam superheat
- the latter superheated steam is suitable as feed to a steam turbine.
- the fuel gas may be pre-heated before introduction into a burner in the radiant section and before contacting with the pre-heated oxygen containing stream therein.
- Such fuel gas pre-heating may be achieved by indirect heat exchange outside the cracker furnace between flue gas from the convection section and the fuel gas, or by indirect heat exchange inside the cracker furnace between flue gas in the convection section and the fuel gas.
- Example A (according to the invention) is further described.
- Example A is described and compared with the Reference Example. All of said Examples concern a process for producing olefins from a feed stream containing saturated hydrocarbons by pyrolytic cracking of the hydrocarbons in a steam cracker furnace.
- the total duty to be provided by fuel gas fed to the steam cracker furnace comprising a convection section and a radiant section for pyrolytic cracking of the hydrocarbons from above-mentioned feed stream
- KTI/Technip Energy EFPS Ethylene furnace program sets containing embedded SpyroSuite® for reaction kinetics
- a number of cracking furnace parameters was kept constant, including (but not limited to): (i) the duty of the radiant section required for above- mentioned pyrolytic cracking; (ii) the ratio of dilution steam to feed (i.e. hydrocarbons) in the radiant section;
- Figure 1 shows a steam cracker furnace 1 comprising a convection section 2 and a radiant section 3, wherein convection section 2 comprises eight banks 4 to 11.
- a feed stream 12a containing saturated hydrocarbons is sent to an UFPH bank 4 wherein it is heated by indirect heat exchange with flue gas originating from radiant section 3, said flue gas having an inlet temperature of 140 °C and an outlet temperature of 100 °C.
- inlet an inlet to the UFPH bank 4 is meant and by “outlet” an outlet from the UFPH bank 4 is meant.
- the stream 12b exiting UFPH bank 4 is partially vaporized and is mixed with a 1 st portion of superheated dilution steam (not shown in Figure 1) which dilution steam is supplied in to DSSH bank 9 (from an upstream dilution steam generator outside furnace battery limit (not shown in Figure 1) and is superheated by indirect heat exchange with flue gas having an inlet temperature of 955 °C and an outlet temperature of 860 °C) and which dilution steam has a pressure of about 5 to 6 barg and a temperature of about 700 °C, and sent to an LFPH bank 6 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 360 °C and an outlet temperature of 250 °C.
- the stream 12c exiting LFPH bank 6 is fully vaporized and has a temperature of 300 °C.
- Stream 12c is then mixed with a 2 nd portion of superheated dilution steam (not shown in Figure 1) from DSSH bank 9, and sent to MPH (or HTC-1) bank 7 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 630 °C and an outlet temperature of 360 °C.
- the stream 12d exiting MPH bank 7 is then sent to HTC-2 bank 10 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 1025 °C and an outlet temperature of 955 °C.
- the stream 12e exiting HTC-2 bank 10 is then sent to HTC-3 bank 11 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 1165 °C and an outlet temperature of 1025 °C.
- the stream 12f exiting HTC-3 bank 11 has a temperature of 600 °C and is sent to radiant section 3 which comprises multiple burners (not shown in Figure 1) wherein air (fed via stream 13) and a fuel gas comprising methane and hydrogen (fed via stream 14) are contacted, and the fuel gas is combusted resulting in the release of above-mentioned flue gas into radiant section 3.
- the air fed to said burners via stream 13 has a temperature of 27 °C.
- the temperature of the flue gas leaving radiant section 3 and entering convection section 2 is 1165 °C.
- stream 12f is further heated to a temperature of 810 °C. At said temperature, saturated hydrocarbons from stream 12f are pyrolytically cracked and olefins are produced.
- the olefins containing effluent which leaves radiant section 3 via stream 12g and which has a temperature of about 810 °C, is rapidly cooled in TLE 15 by indirect heat exchange as further described below.
- the cooled effluent in stream 12h having a temperature of 450 to 500 °C is then sent to a work-up section (not shown in Figure 1) in which several products are separated from the effluent.
- BFW utility water having a pressure of 135 bara and a temperature of 117 °C is sent via stream 16a to an ECO bank 5 wherein it is heated and vaporised by indirect heat exchange with flue gas having an inlet temperature of 250 °C and an outlet temperature of 140 °C.
- the stream 16b exiting ECO bank 5 and having a temperature of 197°C is then sent to a steam drum (not shown in Figure 1) and the steam from said steam drum is then sent to TLE 15 (the steam drum being thermally coupled to the TLE through a thermosyphon) wherein it is further heated by indirect heat exchange with above-mentioned effluent in stream 12g, resulting in a stream 16c containing superheated steam having a pressure of 115 bara and a temperature of 327 °C.
- Stream 16c is then sent to HPSS bank 8 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 860 °C and an outlet temperature of 630 °C.
- Superheated steam having a temperature of 525 °C in the stream 16d exiting HPSS bank 8 is then used as feed to a steam turbine 17.
- the steam is expanded in various stages, as represented by 17a, 17b, 17c and 17d in Figure 1, wherein HP steam (40 bara; 350 °C), MP steam (19 bara; 260 °C), LP steam (7 bara; 170 °C) and sub atmospheric steam (0.08 bara; 41 °C), respectively, are generated.
- power 18 is generated to drive compressors in above-mentioned work-up section.
- the HP steam from HP stage 17a is sent completely to MP stage 17b, and the MP steam from MP stage 17b is sent completely to LP stage 17c.
- the LP steam from LP stage 17c is split, and one portion in stream 16e is extracted from steam turbine 17 and another portion is sent to the final stage 17d from which above-mentioned sub atmospheric steam is extracted into stream 16f which is sent to a steam turbine exhaust condenser 19.
- stream 16f is cooled and condensed resulting in a stream 16g containing condensed water and having a pressure of 0.1 bara and a temperature of 52 °C. Cooling water having ambient temperature 34 °C is provided to condenser 19 via stream 19a and warm cooling water is removed therefrom via stream 19b which may have to be discharged into the environment.
- Streams 16e and 16g are combined and air is removed therefrom (not shown in Figure 1) and the resulting water stream having a pressure of 5 bara and a temperature of 115 °C is pressurized to a pressure of 135 bara and sent as BFW (utility water) in stream 16a having a temperature of 117 °C to convection section 2 of cracker furnace 1, as described above.
- BFW utility water
- Example A according to the present invention, the procedure of the Reference Example is followed except that the set-up as shown in Figure 2 is applied as further described below and in Table 2, wherein the differences between Example A and the Reference Example are as follows.
- An air stream 13a having a temperature of 27 °C is sent to an APH-1 bank 4 wherein it is pre-heated by indirect heat exchange with flue gas originating from radiant section 3, said flue gas having an inlet temperature of 210 °C and an outlet temperature of 100 °C.
- a pre-heated feed stream 12a containing saturated hydrocarbons is sent to an "feed heating in a conventional TEMA heat exchangers where it is preheated to 192 °C, and then sent to a UFPH bank 5 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 270 °C and an outlet temperature of 210 °C .
- the stream 12b exiting UFPH bank 5 is partially vaporized and is mixed with a 1 st portion of superheated dilution steam generated in DSSH bank 9 (from a water feed stream and by indirect heat exchange with flue gas having an inlet temperature of 915 °C and an outlet temperature of 800 °C) and which dilution steam has a pressure of 5 to 6 Bara and a temperature of 700 °C and sent to an MPH (or HTC-1) bank 7 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 500 °C and an outlet temperature of 300 °C.
- the stream 12c exiting MPH bank 7 is fully vaporized and has a temperature of about 410 °C.
- Stream 12c is then mixed with a 2 nd portion of superheated dilution steam from DSSH bank 9, and sent to HTC- 2 bank 10 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 1000 °C and an outlet temperature of 915 °C.
- the stream 12d exiting HTC-2 bank 10 is then sent to HTC-3 bank 11 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 1160 °C and an outlet temperature of 1000 °C.
- the stream 12e exiting HTC-3 bank 11 has a temperature of 625 °C and is sent to radiant section 3.
- the temperature of the flue gas leaving radiant section 3 and entering convection section 2 is 1160 °C.
- stream 12e is further heated to a temperature of 810°C.
- the olefins containing effluent in stream 12f has a temperature of about 803 °C and is rapidly cooled in TLE 15 by indirect heat exchange as further described below.
- the cooled effluent in stream 12g having a temperature of about 450 to 500 °C is then sent to the work-up section.
- pre-heated BFW (utility water) having a pressure of 135 bara and a temperature of 250 °C is sent via stream 16a to the steam drum and the saturated BFW from said steam drum is then sent to TLE 15 wherein it is further heated by indirect heat exchange with above-mentioned effluent in stream 12f, resulting in a stream 16b containing superheated steam having a pressure of about 115 bara and a temperature of 327 °C.
- Stream 16b is then sent to HPSS bank 8 wherein it is further heated by indirect heat exchange with flue gas having an inlet temperature of 800 °C and an outlet temperature of 500 °C.
- Superheated steam having a temperature of 525 °C in the stream 16c exiting HPSS bank 8 is then used as feed to steam turbine 17.
- HP steam from HP stage 17a (of steam turbine 17) is split, and one portion in stream 16dl is extracted from steam turbine 17 and another portion in stream 16d2 is sent to MP stage 17b.
- the MP steam from MP stage 17b is also split, and one portion in stream 16el is extracted from steam turbine 17 and another portion in stream 16e2 is sent to LP stage 17c.
- Stream 16el is further split into streams 16ela and 16elb.
- stream 16f is further split into streams 16fl and 16f2.
- the LP steam from LP stage 17c is also split, and one portion in stream 16f is extracted from steam turbine 17 and another portion is sent to the final stage 17d from which the sub-atmospheric steam is extracted into stream 16g which is sent to steam turbine exhaust condenser 19.
- stream 16g is cooled and condensed resulting in a stream 16h containing condensed water and having a pressure of 0.1 bara and a temperature of 52 °C.
- Streams 16fl and 16h are combined and air is removed therefrom and the resulting water stream having a pressure of 5 bara and a temperature of 115 °C is pressurized to a pressure of 135 bara and sent as BFW (utility water) in stream 16i having a temperature of 117°C to a 1 st heat exchanger 20 wherein it is pre-heated by indirect heat exchange with MP steam from stream 16ela, resulting in BFW stream 16j having a temperature of 205 °C.
- BFW utility water
- BFW stream 16j is then sent to a 2 nd heat exchanger 21 wherein it is further heated by indirect heat exchange with HP steam from stream 16dl, resulting in BFW stream 16a having a temperature of 250 °C which is sent to TLE 15, as described above.
- the heat exchangers 20-23 outside of the cracker furnace can be conventional TEMA (Tubular Exchanger Manufacturers Association) classified heat exchangers, or alternative non tubular technology as for example plate and frame type.
- a feed stream 12' containing saturated hydrocarbons is sent to a 1 st heat exchanger 22 wherein it is pre heated by indirect heat exchange with LP steam from stream 16f2, resulting in stream 12" having a temperature of 156 °C.
- Stream 12" is then sent to a 2 nd heat exchanger 23 wherein it is further heated by indirect heat exchange with MP steam from stream 16elb, resulting in stream 12a having a temperature of 192 °C which is sent to convection section 2 of cracker furnace 1, as described above.
- Example A and the Reference Example are compared in terms of energy savings.
- Example A wherein in accordance with the present invention (i) the hydrocarbons feed stream is pre-heated outside the cracker furnace (in specific, in heat exchangers 22 and 23 in Fig.
- Example A the total fuel gas duty required to produce the same amount of the same chemicals (including olefins) from the same amount of the same saturated hydrocarbons in the feed, in Example A is reduced as compared to the Reference Example. Accordingly, the amount of fuel gas needed is likewise reduced in Example A to the same extent as compared to the Reference Example.
- the above-mentioned comparison has shown that in addition to above-mentioned pre-heating of the hydrocarbons feed stream outside the cracker furnace and pre-heating the air feed stream, also pre-heating the utility water outside the cracker furnace (in specific, pre-heating BFW in heat exchangers 20 and 21 in Fig. 2) before pressurized steam is generated therefrom (in specific, in TLE 15 in Fig. 2), even further reduces above-mentioned total required fuel gas duty and accordingly amount of fuel gas needed, by a total reduction percentage of 16.2% (see Table 2 above).
- the above-mentioned comparison has shown that not only the total required fuel gas duty is reduced by the present invention, thereby reducing the amount of fuel gas needed and also reducing the amount of carbon dioxide emitted into the atmosphere e.g. in case such fuel gas comprises methane, but simultaneously the amount of warm cooling water (in specific, in stream 19b in Fig. 2) produced by cooling the sub-atmospheric steam in the exhaust stream (in specific, stream 16g in Fig.
- pressurized steam (utility water) from the steam cracker furnace is used to provide power through expansion of that steam, is also reduced so that the amount of warm cooling water that may have to be cooled in cooling towers is likewise reduced, because part of the expanded steam is extracted from the steam turbine in order to provide a heat source for above-mentioned pre-heating of the hydrocarbons feed stream and utility water outside the cracker furnace.
- the reduction in the amount of warm cooling water is substantial as indicated by the 33.3% reduction in the flow rate of condensed water in the exhaust stream from the steam turbine (see Table 2 above).
- less power is delivered in Example A as compared to the Reference Example, because in Example A, a relatively large part of the steam is not used to provide turbine shaft power, but to pre-heat furnace hydrocarbons feed and utility water.
- this loss in power provided by the steam turbine is, surprisingly and advantageously, only relatively small (i.e. 14.8% less; see Table 2 above).
- e-motor electrically driven motor
- the electrical power may be provided by renewable, non-fossil energy resources, in addition to above-mentioned steam turbine.
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Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4479869A (en) | 1983-12-14 | 1984-10-30 | The M. W. Kellogg Company | Flexible feed pyrolysis process |
US20170022429A1 (en) * | 2014-02-25 | 2017-01-26 | Joris Van Willigenburg | A process for increasing process furnaces energy efficiency |
WO2018229267A1 (en) | 2017-06-16 | 2018-12-20 | Technip France | Cracking furnace system and method for cracking hydrocarbon feedstock therein |
WO2021052642A1 (en) * | 2019-09-20 | 2021-03-25 | Technip France | Cracking furnace system and method for cracking hydrocarbon feedstock therein |
US20210171836A1 (en) * | 2019-12-09 | 2021-06-10 | Coolbrook Oy | Heat Integration in a Hydrocarbon Processing Facility |
-
2022
- 2022-06-20 WO PCT/EP2022/066711 patent/WO2022268706A1/en active Application Filing
- 2022-06-20 EP EP22734946.1A patent/EP4359491A1/en active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4479869A (en) | 1983-12-14 | 1984-10-30 | The M. W. Kellogg Company | Flexible feed pyrolysis process |
US20170022429A1 (en) * | 2014-02-25 | 2017-01-26 | Joris Van Willigenburg | A process for increasing process furnaces energy efficiency |
WO2018229267A1 (en) | 2017-06-16 | 2018-12-20 | Technip France | Cracking furnace system and method for cracking hydrocarbon feedstock therein |
WO2021052642A1 (en) * | 2019-09-20 | 2021-03-25 | Technip France | Cracking furnace system and method for cracking hydrocarbon feedstock therein |
US20210171836A1 (en) * | 2019-12-09 | 2021-06-10 | Coolbrook Oy | Heat Integration in a Hydrocarbon Processing Facility |
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