WO2023025737A1 - Appareil de craquage chauffé électriquement et dispositif de récupération d'énergie thermique - Google Patents

Appareil de craquage chauffé électriquement et dispositif de récupération d'énergie thermique Download PDF

Info

Publication number
WO2023025737A1
WO2023025737A1 PCT/EP2022/073363 EP2022073363W WO2023025737A1 WO 2023025737 A1 WO2023025737 A1 WO 2023025737A1 EP 2022073363 W EP2022073363 W EP 2022073363W WO 2023025737 A1 WO2023025737 A1 WO 2023025737A1
Authority
WO
WIPO (PCT)
Prior art keywords
thermal energy
energy recovery
recovery assembly
feed
inner tube
Prior art date
Application number
PCT/EP2022/073363
Other languages
English (en)
Inventor
Raul VELASCO PELAEZ
Scott A. Stevenson
Michael Edward HUCKMAN
Arno Johannes Maria OPRINS
Joseph William SCHROER
Jens HETZER
Dr. Jörg WEIDENFELLER
Dr. Michael OLBRICHT
Andreas LINNENKOHL
Thorsten SCHLIETER
Original Assignee
Sabic Global Technologies B.V.
Arvos Gmbh
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Sabic Global Technologies B.V., Arvos Gmbh filed Critical Sabic Global Technologies B.V.
Publication of WO2023025737A1 publication Critical patent/WO2023025737A1/fr

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
    • C10G9/002—Cooling of cracked gases
    • 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
    • C10G9/24—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/10—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically
    • F28D7/103—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically consisting of more than two coaxial conduits or modules of more than two coaxial conduits
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • F28D7/163—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing
    • F28D7/1669—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing the conduit assemblies having an annular shape; the conduits being assembled around a central distribution tube
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/02—Header boxes; End plates
    • F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
    • F28F9/027—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits in the form of distribution pipes
    • F28F9/0273—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits in the form of distribution pipes with multiple holes

Definitions

  • the present disclosure relates to systems and methods for transferring thermal energy and, more particularly, to energy recovery devices for transferring thermal energy from a hot effluent to a feed for a reactor furnace.
  • natural gas and/or light gas may be combusted in gas-fired steam cracking furnaces.
  • Combustion of the hydrocarbons in the gas-fired steam cracking furnace forms carbon dioxide, which is emitted as part of flue gas from the gas-fired steam cracking furnace.
  • Such emissions may be undesirable in view of current environmental considerations.
  • Olefins are a major chemical building block and may often be produced in large quantities, from several hundred thousand tons per year in a small cracker to two million tons per year or more at a single large olefin production facility. As a result, the production of olefins using gas-fired steam cracking furnaces may result in an undesirably high emission of carbon dioxide.
  • the combustion gases can only supply heat to the cracking reaction when the temperature exceeds the temperature of reaction, for example, from 650°C to 850°C. Once the gases have cooled below this temperature, there may be a desire to extract as much of the remaining heat as possible to achieve energy-efficient operation of the plant. This heat is conventionally recovered in a so-called convection section. Often the energy is used to preheat the reactor feeds and diluent steam to the temperature needed for the cracking reaction to occur. [0005] In olefin production, once the feed is cracked, the reactor effluent should be cooled before further processing of the cracked gas.
  • the initial cooling occurs quickly to reduce or prevent side reactions in the reactor effluent while it is still at relatively high temperatures.
  • the heat of the reactor effluent should be recovered to the greatest extent possible and used elsewhere in the process.
  • this quenching and cooling takes place in transfer line exchangers (TLE), where the reactor effluent is cooled by exchanging heat with liquid water to produce high- pressure steam. Cooling by exchanging heat with boiling water has the advantage that heat transfer is generally more rapid than when cooling against a gas, sometimes five or even ten times faster for the same exchanger geometry.
  • This steam may be used to power steam turbines or other auxiliaries. For example, the steam is commonly used to power the cracked gas compressor, one or more of the refrigeration compressors, or one or more pumps.
  • Electrified steam cracking includes the use of cracking furnaces that are at least in part directly or indirectly heated by electricity. Electrified steam cracking furnaces have reduced emissions as compared to gas-fired cracking furnaces.
  • electrified steam cracking furnaces introduce new technical challenges that must be overcome.
  • One consequence of using an electrified steam cracking furnace is the elimination of hot flue gas from the combustion of fuel in the gas-fired cracking furnace, so that heating typically supplied by the hot flue gas, including feed preheating, must be supplied another way.
  • a second consequence is the need for different energy integration within the cracking process.
  • Rotating equipment such as compressors and pumps are easily powered by electricity; moreover, the efficiency of operation of such equipment with electricity is much higher than with steam, with energy efficiencies of greater than 90% commonly achieved when using electricity as compared to 30 to 50% typically obtained when using steam. Therefore, in an electric steam cracking process there is considerable incentive to power these devices using electricity. This means that the energy currently recovered when cooling the reactor effluent can no longer be used for powering pumps and compressors; instead there is a need to find a different use for this energy so that the overall energy efficiency of the process can be maintained at a high level.
  • Applicant has identified a need for systems and methods for using the energy obtained from quenching hot reactor effluent while still quenching the cracked gas quickly enough to prevent further reaction. Applicant has also identified a need for systems and methods for preheating a feed for an electrically powered furnace.
  • a method to produce olefins including supplying a hydrocarbon feed to an outer tube of a thermal energy recovery assembly; heating the hydrocarbon feed in the outer tube of the thermal energy recovery assembly to output a preheated hydrocarbon feed; supplying the preheated hydrocarbon feed to an electrically powered cracking furnace comprising a reaction zone to heat the preheated hydrocarbon feed; cracking the preheated hydrocarbon feed in the reaction zone of the electrically heated cracking furnace using heat generated by electricity to output hot reactor effluent comprising cracked hydrocarbons and olefins; supplying the hot reactor effluent to an inner tube of the thermal energy recovery assembly; and cooling the hot reactor effluent in the inner tube of the thermal energy recovery assembly by transferring heat to the hydrocarbon feed.
  • the method may also include supplying an additional feed different than the hydrocarbon feed to the outer tube of the thermal energy recovery assembly; and heating the additional feed by transferring heat from the hot reactor effluent to the additional feed via the thermal energy recovery assembly.
  • the method may include withdrawing a partially preheated hydrocarbon feed from the outer tube of the thermal energy recovery assembly; feeding the partially preheated hydrocarbon feed to the thermal energy recovery assembly; and further heating the partially preheated hydrocarbon feed by transferring heat from the hot reactor effluent via the thermal energy recovery assembly, to output the preheated hydrocarbon feed.
  • the method may include cooling the hot reactor effluent at a rate of at least 2.5 degrees Kelvin/millisecond, at least 3.5 degrees Kelvin/millisecond, or at least 4.5 degrees Kelvin/millisecond.
  • a pressure drop of the hot reactor effluent passing through the thermal energy recovery assembly is less than 0.35 bar, less than 0.30 bar, less than 0.25 bar, less than 0.20 bar, or less than 0.15 bar.
  • a residence time of the hot reactor effluent within the thermal energy recovery assembly may be less than 100 milliseconds, less than 95 milliseconds, less than 90 milliseconds, less than 85 milliseconds, is less than 83 milliseconds, or is less than 80 milliseconds.
  • a pressure drop of the feed passing through the thermal energy recovery assembly may be from 2 to 15 bar, from 2.5 to 10 bar, from 3 to 8 bar, from 3 to 10 bar, from 4 to 9 bar, or from 5 to 8 bar.
  • a thermal energy recovery assembly may include an inner tube with a first inlet configured to receive the hot reactor effluent from the electrically powered cracking furnace; and an outer tube disposed about the inner tube to enclose an annulus about the inner tube, the annulus including a second inlet configured to receive the hydrocarbon feed.
  • the annulus may include at least one heat transfer enhancement to enhance heat transfer from the inner tube to the annulus.
  • the annulus may include a first stage, and the at least one heat transfer enhancement that includes one or more of impingement, turbulence promotion, high-shear- inducing geometry, or increased surface area.
  • the annulus may include a plate impingement between an upstream end and a downstream end
  • the plate impingement may include: a first channel having a stage inlet at the upstream end and being closed to flow at the downstream end; a second channel having a stage outlet at the downstream end, the second channel being disposed between the first channel and the inner tube; a wall separating the first channel from the second channel, the wall defining openings to fluidly connect the first channel and the second channel; and the plate impingement being configured to receive feed through the stage inlet, flow feed from the first channel to the second channel via the openings of the wall, and causing flow of the feed to impinge onto an outer surface of the inner tube and exhaust feed through the stage outlet of the second channel.
  • the annulus may include a piccolo impingement
  • the piccolo impingement may include: an upstream divider disposed about the inner tube and within the outer tube; a downstream divider disposed about the inner tube and within the outer tube downstream of the upstream divider within the annulus, the downstream divider defining at least one stage outlet; a chamber defined within the outer tube and about the inner tube between the upstream divider and the downstream divider; and piccolo tubes offset from the inner tube, the piccolo tubes extending through the chamber from the upstream divider to the downstream divider, the piccolo tubes including a stage inlet for receiving incoming feed, the piccolo tubes including a plurality of openings defined therein, the piccolo impingement being configured to receive feed from the stage inlets, flow feed from the piccolo tubes into the chamber via the plurality of openings, and exhaust feed from the chamber via the at least one stage outlet.
  • the annulus may include at least a first stage and a second stage, wherein the first stage and the second stage may be in series, wherein both stages may include at least one heat transfer enhancement.
  • the inner tube may include a heat transfer enhancement including one or more of impingement, turbulence promotion, high-shear-inducing geometry, or increased surface area.
  • the thermal energy recovery assembly may include a plurality of inner tubes parallel with one another with each inner tube disposed within an outer tube, each outer tube may have one or more of impingement, turbulence promotion, high-shear- inducing geometry, or increased surface area to enhance heat transfer from the inner tube to an annulus defined within the outer tube.
  • FIG. 1 is a schematic view of a portion of an example furnace assembly for heating a feed to provide a hot reactor effluent in accordance with embodiments of the present disclosure
  • FIG. 2A is a partial schematic section side view of an example thermal energy recovery assembly according to embodiments of the present disclosure
  • FIG. 2B is a partial schematic section end view taken along line B-B of the example thermal energy recovery assembly shown in FIG. 2A according to embodiments of the present disclosure
  • FIG. 3A is a partial schematic perspective view of another example thermal energy recovery assembly according to embodiments of the disclosure.
  • FIG. 3B is a partial schematic section end view taken along line B-B of the example thermal energy recovery assembly shown in FIG. 3A according to embodiments of the present disclosure
  • FIG. 4A is a schematic section view of an example inner tube including example rounded projections on an interior surface of the inner tube according to embodiments of the disclosure;
  • FIG. 4B is a schematic section view of another example inner tube including example rectangular projections on an interior surface of the inner tube according to embodiments of the disclosure;
  • FIG. 5 is a block diagram of an example method to produce olefins according to embodiments of the disclosure.
  • FIG. 1 schematically illustrates an example furnace assembly 10 for heating a feed to provide a hot reactor effluent according to embodiments of the disclosure.
  • the furnace assembly 10 may be used for producing olefins from hydrocarbons.
  • the furnace assembly 10 may include an electrically powered furnace 20 and a thermal energy recovery assembly 30.
  • the phrase “hot reactor effluent” refers to reactor effluent that is downstream of the furnace 20 and is being cooled from the temperature at which reactor effluent exited the furnace 20.
  • the thermal energy recovery assembly 30 may include one or more stages, for example, a first stage 31a, a second stage 31b, and a third stage 31c, for example, as shown in FIG. 1.
  • the stages may have substantially the same structural configuration, and in some embodiments including more than one stage, one or more of the stages may have a structural configuration that differs from the structural configuration of other stages.
  • two or more of the stages may be in series relative to one another (e.g., physically and/or with respect to processing) (see, e.g., FIG.
  • the furnace 20 may be configured to receive a feed and heat the feed to a reaction temperature to provide a hot reactor effluent.
  • the feed and/or the effluent may be in the form of a liquid, a gas, or a combination thereof.
  • the furnace 20 may be an electrically powered cracking furnace and the feed may be, or include, hydrocarbons for cracking in the furnace 20 to provide a hot reactor effluent including cracked hydrocarbons, for example, in an at least partially gaseous state (e.g., a completely gaseous state).
  • the furnace 20 may be configured to heat the feed to a cracking temperature to break the hydrocarbons into desired products that may be exhausted from the furnace 20 as a hot reactor effluent.
  • the feed may include, for example, ethane, propane, butane, condensate, light naphtha, heavy naphtha, gas oil, pyrolysis oil, materials derived from processing refinery streams, Fischer-Tropsch products, plastic waste, and/or biofeedstocks.
  • the feed may additionally include steam.
  • the furnace 20 may be configured to receive the feed into one or more reactor zones or reactor chambers 25 (for example, a cracker tube or a cracking coil) via a reactor feed line 22 and exhaust the hot reactor effluent via a reactor effluent line 28.
  • the furnace 20 may be electrically heated to a cracking temperature, for example, such that the feed substantially continuously flows into the reactor chamber(s) 25 via the reactor feed line 22 and out of the reactor chamber(s) 25 as hot reactor effluent via the reactor effluent line 28.
  • the reactor chamber(s) 25 may be heated directly or indirectly by electrical power.
  • the feed may be preheated to a temperature closer to the cracking temperature of the feed prior to (e.g., upstream relative to) entering the reactor chamber(s) 25.
  • Reactor feed line 22 and reactor effluent line 28 may be configured to traverse additional equipment, for example heat transfer equipment, not depicted in Fig. 1.
  • the thermal energy recovery assembly 30, in some embodiments, may be, or include, a gas-to-gas energy recovery device or heat exchanger.
  • the thermal energy recovery assembly 30 may be configured to receive the hot reactor effluent from the reactor chamber(s) 25 and quench the hot reactor effluent to a quenched temperature to preserve the desired products within the reactor effluent and/or to prevent side reactions from occurring within the reactor effluent, for example, as the hot reactor effluent cools.
  • a single thermal energy recovery assembly 30 may receive hot reactor effluent from multiple reactor chambers 25.
  • a single reactor chamber 25 may provide hot reactor effluent to multiple thermal energy recovery assemblies 30.
  • the ratio between the number of reactor chambers 25 and the number of thermal energy recover assemblies 30 may be in a range of 0.1 to 10, for example, a range of 0.5 to 2.
  • the hot reactor effluent enters the thermal energy recovery assembly 30 at a temperature of at least 575°C, at least 600°C, at least 610°C, at least 620°C, at least 625°C, at least 630°C, at least 640°C, at least 650°C, at least 700°C, at least 750°C, at least 800°C, or at least 850°C.
  • the thermal energy recovery assembly 30 may utilize the feed as a cooling medium, for example, prior to the feed entering the reactor chamber 25 (e.g., upstream of the reactor chamber 25).
  • the feed may be preheated to a temperature closer to the cracking temperature thereof (e.g., to a temperature of at least 350°C, at least 375°C, at least 400°C, at least 450°C, at least 500°C, or at least 550°C).
  • the thermal energy recovery assembly 30 may be configured to preheat the feed over a cracking temperature, for example, such that cracking begins to occur in the thermal energy recovery assembly 30, for example, when the feed is preheated to a temperature greater than 650°C.
  • quenched reactor effluent refers to reactor effluent that has passed through the thermal energy recovery assembly 30.
  • the hot reactor effluent may additionally be partially cooled or quenched before or after passing through the thermal energy recovery assembly 30.
  • the preheated feed may be further heated (for example, by means of a fired heater or an electrical heater) before entering the reactor chamber.
  • a thermal energy recovery assembly 30 may be configured to recover thermal energy from hot reactor effluent to heat a feed to an electrically-powered reactor furnace.
  • the thermal energy recovery assembly 30 may include an inner tube 34 and an outer tube 40.
  • the inner tube 34 may include a first inlet that is configured to receive hot reactor effluent from an electrically-powered reactor furnace.
  • the outer tube 40 may be disposed about the inner tube 34 to enclose an annulus 44 about the inner tube 34.
  • the “annulus 44” may, or may not, be defined by inner and outer circles to result in an annular cross-section having inner and outer circular boundaries.
  • the inner and/or outer boundaries of the cross-section may have shapes other than circular, such as triangular, rectangular, polygonal, elliptical, oval-shaped, etc.
  • the central axis of the inner tube may coincide with the central axis of the outer tube.
  • the central axis of the inner tube may be offset from the central axis of the outer tube.
  • the term “annular” (and derivations thereof) may be interpreted similarly.
  • the annulus 44 may include a second inlet that is configured to receive a feed to the electrically- powered reactor furnace.
  • the annulus 44 may be configured to use the feed for the electrically- powered reactor furnace as a cooling medium to recover thermal energy from the hot reactor effluent prior to the feed being supplied to the electrically-powered reactor furnace.
  • the annulus 44 may be configured to enhance heat transfer from the hot reactor effluent to the feed.
  • hot reactor effluent may reach a first inlet via an effluent gas inlet chamber or other connector.
  • cooling may be supplied to a feed gas inlet chamber or other connector.
  • the effluent gas inlet chamber may connect one or more than one reaction chambers to one or more than one inner tube.
  • a header may be provided to connect the feed to more than one annulus 44.
  • cooled cracked gas from more than one inner tube 34 may be collected using a header.
  • heated feed from more than one annulus 44 may be combined via a header.
  • multiple annuli 44 may be contained in a single mechanical device, which may receive hot effluent from multiple cracking coils via a gas inlet chamber or other connector, and cold feed from a feed header.
  • the residence time and/or the pressure drop of the reactor effluent in the thermal energy recovery assembly 30 may be influential on the process and/or the products achieved by the heating process in the furnace assembly 10. Both the residence time and the pressure drop occurring as the hot reactor effluent passes through the thermal energy recovery assembly 30 may be influential on ethylene selectivity of products produced by the furnace assembly 10.
  • the residence time may be defined as the time that the hot reactor effluent exceeds a temperature greater than its cracking temperature, for example, greater than 650°C.
  • both the residence time and the pressure drop may be balanced during the quenching of the hot reactor effluent, for example, to preserve the ethylene selectivity of the reactor effluent.
  • an increased pressure drop in the thermal energy recovery assembly can affect the selectivity as a result of an increased pressure in cracking coils of the furnace assembly 10 which changes selectivity of the cracking reaction in the furnace assembly 10.
  • a longer residence time may allow for additional side reactions in the thermal energy recovery assembly 30.
  • the thermal energy recovery assembly 30 may be configured to quench the hot reactor effluent received from the furnace 20 using the feed to the furnace 20 as a cooling medium for the hot reactor effluent, for example, and such that the feed is preheated by the hot reactor effluent prior to entering the reactor chamber 25. For example, as shown in FIG.
  • the thermal energy recovery assembly 30 may receive the feed through a cold feed line 32 and provide preheated feed to the reaction chamber 25 through the reactor feed line 22.
  • the thermal energy recovery assembly 30 may receive hot reactor effluent from the reactor effluent line 28 and provide quenched reactor effluent to a quenched effluent line 38.
  • the thermal energy recovery assembly 30 may be configured to operate as a gas-to-gas heat exchanger to exchange heat from the hot reactor effluent to the feed.
  • a gas-to-gas heat exchanger to exchange heat from the hot reactor effluent to the feed.
  • liquid-to-gas heat exchangers e.g., steamgenerating heat exchangers using boiling water as a relatively low-temperature cooling medium, typically used with gas-fired cracking furnaces
  • additional design features for thermal energy recovery assembly 30 may be desired, as described in some of the exemplary embodiments below.
  • an example thermal energy recovery assembly 30 having a tube-in-tube design with a hot reactor effluent flowing through an inner tube 34 (e.g., a central tube), and the feed flowing through an annulus 44 at least partially defined by the inner tube 34 and an outer tube 40.
  • the inner tube 34 is disposed about a central axis of the thermal energy recovery assembly 30.
  • the inner tube 34 may be disposed about the central axis or offset from the central axis of the thermal energy recovery assembly 30.
  • the thermal energy recovery assembly 30 may be a co-current heat exchanger or counter- current heat exchanger (e.g., as shown) with the hot reactor effluent flowing through the thermal energy recovery assembly 30 in a first direction and the feed flowing through the thermal energy recovery assembly 30 in a second direction opposite the first direction.
  • the inner tube 34 may include an inlet 33 and an outlet 35, with the hot reactor effluent entering through the inlet 33, flowing through the inner tube 34, and exiting through the outlet 35.
  • the annulus 44 may include an inlet 43 and an outlet 45, with the feed entering through the inlet 43, flowing through the annulus 44, and exiting through the outlet 45 as preheated feed.
  • the hot reactor effluent enters the thermal energy recovery assembly 30 at the inlet 33 at a point adjacent to where the feed, at its highest temperature after being heated by the reactor effluent, exits the thermal energy recovery assembly 30 through the outlet 45 as preheated feed.
  • the reactor effluent e.g., a quenched reactor effluent
  • at its lowest temperature after heating the feed exits the thermal energy recovery assembly 30 at the outlet 35 as quenched reactor effluent at a point adjacent to where the feed, at its lowest temperature prior to being heated by the hot reactor effluent, enters the thermal energy recovery assembly 30 through the inlet 43.
  • the hot reactor effluent enters the thermal energy recovery assembly 30 at its highest temperature at the point where the feed exits the thermal energy recovery assembly 30 at its highest temperature, and the reactor effluent exits the thermal energy recovery assembly 30 at its lowest temperature where the feed enters the thermal energy recovery assembly 30 at its lowest temperature.
  • the thermal energy recovery assembly 30 may be a co-current heat exchanger with the reactor effluent and the feed flowing in the same direction within the thermal energy recovery assembly 30. In some embodiments, if the thermal energy recovery assembly 30 is made up of more than one stage, some stages may be co-current and others may be counter-current.
  • the inner tube 34 may be or include a bare or plain tube with a smooth inner surface.
  • the inner tube 34 may include heat transfer enhancements that promote turbulence or increase a surface area of the inner tube 34.
  • the inner tube 34 may include velocity rods or other turbulence-promoting structures.
  • the inner tube 34 may include fins (for example, straight and/or rifled fins, rectangular and/or rounded in cross-section) or other surfaces to increase a surface area in contact with the reactor effluent flowing through the inner tube 34.
  • Such heat transfer enhancements within the inner tube 34 may decrease the residence time of the reactor effluent.
  • the heat transfer enhancements may increase a pressure drop within the reactor effluent.
  • the inclusion of heat transfer enhancements within the inner tube 34 may be balanced, for example, to reduce pressure drop that may result from heat transfer enhancements.
  • fouling may be expected such that frequent cleaning of the inner tube 34 may be required.
  • the inner tube 34 may be straight or bare to aid in cleaning.
  • sections of the inner tube 34 may be bare, and sections of the inner tube 34 may include heat transfer enhancements, such as the turbulence-promoting structures and/or the areaincreasing features mentioned above.
  • the annulus 44 may include turbulence-promoting structures, such as, for example, winglets, artificial roughness, washboard/grooves, pin fins, and/or dimples. Such structures may increase the rate of heat transfer from the outer surface of the inner tube 34, and/or may increase the pressure drop of the feed traversing the annulus 44. Such structures may be used by themselves as a heat transfer enhancement, or may be used in combination with other heat transfer enhancements, such as, for example, the plate and piccolo impingements described herein.
  • the annulus 44 may include a high-shear-inducing geometry configured to promote high-shear flow, for example, as may result from feed flowing at high velocity, such as greater than 50 meters per second (m/s), or greater than 60 m/s, or greater than 70 m/s, or greater than 80 m/s.
  • the direction of the high-shear feed flow through the annulus is substantially parallel to the inner tube.
  • the high- shear-inducing geometry may include configuring the outer tube such that the spacing between the outside surface of the inner tube 34 and the inside surface of the outer tube 40 is 10 millimeters (mm) or less, 8 mm or less, 6 mm or less, or 4 mm or less.
  • the high shear rate may serve as a heat transfer enhancement by promoting a high rate of heat transfer from the flowing feed to the outside surface of the inner tube 34.
  • heat transfer enhancement by impingement may refer to flow of fluid passing through the outer tube, whose average direction as it proceeds from inlet to outlet may be substantially parallel to the inner tube, being purposely directed to flow toward the inner tube, for example, using geometric features introduced into the annulus.
  • this directed (impinging) flow may, for example, be perpendicular to the inner tube, or directed toward the inner tube at an angle greater than thirty degrees relative to an axis of the inner tube, while its velocity may be relatively greater than a superficial velocity of the outer-tube fluid (for example, the volumetric flow of the outer-tube fluid divided by the area of the annular crosssection between the inner and outer tube).
  • the geometric features that promote impingement may include, for example, nozzles and/or openings oriented toward the inner tube, and/or obstructions placed in a flow path that may redirect fluid from a direction that is more parallel to the inner tube more directly towards the outer surface of the inner tube.
  • These example features may be implemented in a periodic fashion, for example, resulting in impingement zones that occur at intervals along the length and/or the circumference of the inner tube. Applicant has discovered that introduction of such impingement features may increase the rate of heat transfer relative to the rate that would be attained by parallel flow through the outer tube.
  • a ratio of a velocity of an impinging flow to the superficial velocity may be greater than two, greater than five, or greater than ten.
  • the velocity of the impinging flow may be approximated, in the case of nozzles or openings, as the volumetric flow divided by the total flow area defined by the nozzles or openings, through which the flow is directed.
  • the heat transfer enhancement may be found to be more suitable at distances between the impingement-inducing feature (e.g., between nozzles or openings 54) and the inner tube that are from about the diameter to about twelve times the diameter of the nozzles or openings 54, from about the diameter to about ten times the diameter, or from about two times the diameter to about eight times the diameter.
  • Examples of impingement features may include plate impingement and/or piccolo impingement.
  • at least one heat transfer enhancement in a first stage may be the same or different from at least one heat transfer enhancement in a second stage.
  • the annulus 44 (see FIGS. 2 A and 2B) of the thermal energy recovery assembly 30 may include one more structures to promote heat transfer from the reactor effluent in the inner tube 34 to the feed in the annulus 44 of the thermal energy recovery assembly 30.
  • the thermal energy recovery assembly 30 may include plate impingements 50 in the annulus 44 of the thermal energy recovery assembly 30, for example, as shown in FIGS. 2A and 2B, and/or the thermal energy recovery assembly 30 may include piccolo impingements 60 (see also FIG. 3A) in the annulus 44 (see also FIG. 3B) of the thermal energy recovery assembly 30.
  • the plate impingement 50 may include the cooling medium (e.g., the feed) entering a first channel 52 via a stage inlet 43 that may be spaced apart from the inner tube 34, for example, on an outside or outer circumference of the annulus 44 of the thermal energy recovery assembly 30.
  • the cooling medium exits the first channel via one or more nozzles or openings 54 in a wall 55 into a second channel 56 that is in contact with the inner tube 34.
  • the first channel 52 may terminate in a downstream end 58, for example, such that the cooling medium may be forced into the second channel 56 to flow through the annulus 44 and exit through a stage outlet 45 at a downstream end of the second channel 56.
  • the wall 55 separates the first channel 52 from the second channel 56.
  • the thermal energy recovery assembly 30 may include one or more plate impingements 50 disposed along the length thereof. Each plate impingement 50 as shown in FIGS. 2A and 2B may be considered a plate impingement stage with the thermal energy recovery assembly 30 including one or more plate impingement stages in series or parallel with one another.
  • one or more of the nozzles or openings 54 may have a circular cross-section.
  • the diameter of the one or more nozzles or openings 54 may range from about 1 millimeter (mm) to about 15 mm, for example, from about 2 mm to about 10 mm, from about 3 mm to about 8 mm, or from about 4 mm to about 7 mm.
  • the area of the cross-section of the nozzles or openings 54 may substantially correspond to the area of nozzles or openings 54 having a circular cross-section.
  • the nozzles or openings 54 may be circumferentially aligned at different points along the longitudinal length of the wall 55 or they may be circumferentially staggered along the longitudinal length of the wall, for example, in a helically extending manner.
  • wall 55 may be spaced from the outer surface of the inner tube 34 by a distance ranging, for example, when the nozzles or openings 54 have a circular cross-section, from about a distance equal to the diameter of the nozzles or openings 54 to about twelve times the diameter of the nozzles or openings 54, or from about the diameter to about ten times the diameter, from about two times the diameter to about eight times the diameter.
  • the nozzles or openings 54 may be spaced around the circumference of the wall 55.
  • the wall may include, for example, from one to fifteen nozzles or openings 54, which may at least partially depend on the dimensions of the inner tube 34, for example, with relatively more nozzles or openings 54 for relatively larger inner tubes 34.
  • the nozzles or openings 54 may be circumferentially spaced around the inner tube 34, for example, such that the spacing equals pi (i.e., 3.14159) multiplied by the sum of the diameter of the outer surface of the inner tube 34 and two times the distance from the nozzles or openings 54 to the outer surface of the inner tube 34, all of which is divided by the number of nozzles or openings 54 around the circumference.
  • the nozzles or openings 54 may be spaced from one another substantially equally along the longitudinal length of the wall 55 and/or substantially equally circumferentially around the wall 55.
  • the piccolo impingement 60 may include the cooling medium (e.g., the feed) entering one or more piccolo or outer tubes 62 and a chamber 66 defined about the inner tube 34.
  • the chamber 66 may generally define an annulus, such as, for example, the annulus 44 shown in FIGS. 2 A and 2B.
  • the outer tubes 62 may include a stage inlet 43 and may include one or more nozzles or openings 64 configured to allow the cooling medium to flow from the outer tubes 62 into the chamber 66, for example, such that the cooling medium is in contact with the inner tube 34.
  • one or more of the nozzles or openings 64 may be directed at an outer surface of the inner tube 34, for example, as shown in FIG. 3B.
  • the chamber 66 may be defined between a first or upstream divider 65 and second or downstream divider 67.
  • the upstream divider 65 may include openings that allow the cooling medium to enter the outer tubes 62.
  • the downstream divider 67 may terminate a downstream end of each of the outer tubes 62 and may include outlets defined therein that allow the cooling medium to exit the chamber 66 and flow into another set of outer tubes 62 or exit the thermal energy recovery assembly 30.
  • the thermal energy recovery assembly 30 may include one or more piccolo impingements 60 disposed along the length thereof. Each piccolo impingement 60, as shown in FIGS. 3 A and 3B, may be considered a piccolo impingement stage with the thermal energy recovery assembly 30 including one or more piccolo impingements in series or parallel with one another.
  • one or more of the nozzles or openings 64 may have a circular cross-section.
  • the diameter of the one or more nozzles or openings 64 may range from about 1 millimeter (mm) to about 15 mm, for example, from about 2 mm to about 10 mm, from about 3 mm to about 8 mm, or from about 4 mm to about 7 mm.
  • the area of the cross-section of the nozzles or openings 64 may substantially correspond to the area of nozzles or openings 64 having a circular cross-section.
  • the nozzles or openings 64 may be circumferentially aligned relative to the respective outer tubes 62, such that fluid passing through each of the nozzles or openings 64 is directed at the outer surface of the inner tube 34, for example, at an angle of about ninety degrees relative to the outer surface of the inner tube 34.
  • one or more of the nozzles or openings 64 may be circumferentially oriented relative to its respective outer tube 62, such that fluid passing through the nozzle or opening 64 is at a non-perpendicular angle relative to the outer surface of the inner tube 34, ranging, for example, from about ten degrees to about eighty degrees, twenty degrees to about eighty degrees, thirty degrees to about eighty degrees, or about forty-five degrees to about eighty degrees.
  • the nozzles or openings 64 may be located at different points and circumferentially aligned along the length (e.g., in a direction along the longitudinal axis) of the outer tube 62.
  • nozzles or openings 64 may be spaced from the outer surface of the inner tube 34 by a distance ranging, for example, when the nozzles or openings 64 have a circular cross-section, from about a distance equal to the diameter to the nozzle or opening 64 to about twelve times the diameter of the nozzle or opening 64, or from about the diameter to about ten times the diameter, from about two times the diameter to about eight times the diameter.
  • each of the outer tubes 62 may include a single nozzle or opening 64 at each of a plurality of locations along the length of the outer tubes 62.
  • each of the outer tubes 62 may include a number of nozzles or openings 64 ranging from one to fifteen nozzles or openings 64, from one to ten nozzles or openings 64, from one to five nozzles or openings 64 (e.g., four nozzles or openings 64) or from five to ten nozzles or openings 64.
  • the distance between nozzles or openings 64, for example, on a respective outer tube 62 may be defined, such that the distance between adjacent nozzles or openings 64 divided by diameter of the nozzle or opening 64 is greater than or equal to one and less than or equal to twenty.
  • the number of outer tubes 62 in a stage may be between one and twelve, or between two and six.
  • the thermal energy recovery assembly 30 may have a modular design with a plurality of stages along a length thereof.
  • the thermal energy recovery assembly 30 may include one or more plate impingement stages 50 and one or more piccolo impingement stages 60.
  • the thermal energy recovery assembly 30 may include only plate impingement stages 50 or may include only piccolo impingement stages 60.
  • the thermal energy recovery assembly 30 may include plate impingement stages 50, piccolo impingement stages 60, and turbulence-promoting (TP) features or TP stages.
  • TP turbulence-promoting
  • the thermal energy recovery assembly 30 may be used in conjunction with a conventional gas to liquid steam-raising TLE.
  • a conventional TLE may be used to perform the initial quenching of the reactor effluent and then be followed by the thermal energy recovery assembly 30, as long as the reactor effluent enters the thermal energy recovery assembly 30 at a temperature of at least 575°C, at least 600°C, at least 610°C, at least 620°C, at least 630°C, at least 640°C, at least 650°C, at least 700°C, at least 750°C, or at least 800°C, or at least 850°C.
  • the thermal energy recovery assembly 30 may be followed by a conventional TLE, for example, if the thermal energy recovery assembly 30 preheats the feed to at least 350°C, at least 375°C, at least 400°C, at least 425°C, at least 450°C, at least 475°C, at least 500°C, at least 525°C, at least 550°C, at least 575°C, at least 600°C, at least 625°C, or at least 650°C.
  • the furnace assembly 10 may include a conventional TLE before or after the thermal energy recovery assembly 30.
  • the reactor effluent line 28 and/or the quenched effluent line 38 may include a conventional TLE.
  • the conventional gas-to- liquid steam-raising TLE may be part of the same assembly as the thermal energy recovery assembly 30.
  • the thermal energy recovery assembly 30 according to some embodiments may be combined with superheating a steam stream.
  • the characteristics of the stages of the thermal energy recovery assembly 30 may be tuned depending, for example, on the position of the stage within the thermal energy recovery assembly 30.
  • the thermal energy recovery assembly 30 includes plate impingement stages 50
  • the channels 52 and/or 56, the nozzles or openings 54, and/or the length of the plate impingement stages 50 may be sized and dimensioned to optimize heat transfer for conditions at that position along the thermal energy recovery assembly 30.
  • the first channel 56 of a stage 50 at a first position along the thermal energy recovery assembly 30 may have a radial height greater than a radial height of a first channel 56 of a stage 50 at a second position along the thermal energy recovery assembly 30.
  • the nozzles or openings 54 of a stage 50 at the first position may have a diameter less than a diameter of nozzles or openings 54 of a stage 50 at a second position.
  • the radial height may remain substantially equal between one or more stages.
  • the thermal energy recovery assembly 30 includes piccolo impingement stages 60
  • the diameter of the outer tubes 62, the size and/or number of the nozzles 64, and/or the length of the piccolo impingement stages 60 may be sized and dimensioned to optimize heat transfer for conditions at that position along the thermal energy recovery assembly 30.
  • the number of nozzles or openings 54 from stage to stage may be higher, lower, or the same.
  • the number of rows of nozzles or openings 54 may vary from stage to stage.
  • the conditions along the thermal energy recovery assembly 30 may include the temperature of the reactor effluent, the temperature of the feed, the inlet and/or outlet pressure of the reactor effluent, the inlet and/or outlet pressure of the feed, the pressure drop of the reactor effluent along the length of the assembly pressure, the pressure drop of the feed along the length of the thermal energy recovery assembly 30, the temperature difference between the feed and the reactor effluent, the velocity of the reactor effluent, and/or the velocity of the feed.
  • the thermal energy recovery assembly 30 may include stages that are parallel with one another.
  • the thermal energy recovery assembly 30 may activate or deactivate one or more of these parallel stages based on a temperature of hot reactor effluent entering the thermal energy recovery assembly 30 or a temperature of quenched reactor effluent exiting the thermal energy recovery assembly 30.
  • a stage When a stage is activated, hot reactor effluent is flowing through the stage and when a stage is deactivated, hot reactor effluent is prevented from flowing through the stage.
  • the thermal energy recovery assembly 30 may activate another stage or stages and when the quenched reactor effluent exiting the thermal energy recovery assembly 30 may deactivate a stage or stages.
  • the thermal energy recovery assembly 30 may include stages that are in series with one another.
  • the thermal energy recovery assembly 30 may activate or deactivate one or more of these stages based, for example, on the temperature of hot reactor effluent entering the thermal energy recovery assembly 30, the temperature of quenched reactor effluent exiting the thermal energy recovery assembly 30, the temperature of feed entering thermal energy recovery assembly 30, and/or the temperature of feed exiting thermal energy recovery assembly 30.
  • feed may flow through the activated stage, and when a stage is deactivated, feed is prevented from flowing through the deactivated stage.
  • the thermal energy recovery assembly 30 may activate one or more additional stages so that the temperature of the quenched reactor effluent exiting the thermal energy recovery assembly 30 decreases toward the desired temperature, and/or when the quenched reactor effluent exiting the thermal energy recovery assembly 30 is below a desired temperature, the thermal energy recovery assembly 30 may deactivate one or more stages so that the temperature of the quenched reactor effluent exiting the thermal energy recovery assembly 30 increases toward the desired temperature.
  • the thermal energy recovery assembly 30 may include one or more controllers configured to control operation of one or more of the stages, for example, as will be understood by those skilled in the art.
  • the thermal energy recovery assembly 30 may include a plurality of temperature sensors, pressure sensors, flow rate sensors, etc., in communication with the controller, and the controller may use control logic in the form of computer software and/or hardware programs to make control decisions associated with controlling operation of the thermal energy recovery assembly 30, for example, including the one or more stages.
  • the thermal energy recovery assembly 30 may include valves associated with the lines and/or conduits, and the controller may communicate control signals based at least in part on the control decisions to actuators associated with the valves to control the flow of fluid (e.g., gases and/or liquids) and/or heat, and the actuators may be operated according to the communicated control signals to operate the parts of the thermal energy recovery assembly 30.
  • the controller may be supplemented or replaced by human operators at least partially manually controlling the thermal energy recovery assembly 30 to meet desired performance parameters based at least in part on efficiency considerations.
  • the thermal energy recovery assembly 30 may be configured to quench the hot reactor effluent within a residence time and/or with a pressure drop consistent with other quenching devices of a gas-fired cracking furnace. In some embodiments, the thermal energy recovery assembly 30 may be tuned or optimized to be substantially equivalent to, or improved relative to, other types of quenching devices.
  • the thermal energy recovery assembly 30 may be configured such that a residence time, as measured by the time within the thermal energy recovery assembly 30, is less than 100 milliseconds (ms), for example, less than 90 ms, or less than 85 ms (e.g., less than 83 ms); that a pressure drop of the reactor effluent is less than 0.35 bar, for example, less than 0.30 bar, less than 0.25 bar, or less than 0.20 bar (e.g., less than 0.15 bar); and/or that a cooling rate is greater than 2.5 degrees Kelvin (K)/ms, for example, greater than 3.5 K/ms, greater than 4.0 K/ms, greater than 4.5 K/ms, at least 5 degrees K/ms, or at least 5.5 degrees K/ms, for example, where the cooling rate may be defined as the inlet temperature of the hot reactor effluent (in degrees K) minus 923 K, divided by the residence time required for cooling from the temperature of the hot reactor effluent to 923 K
  • Thermal energy recovery assembly 30 may be configured to achieve, in addition to the effluent-side pressure drop and cooling rate performance, a pressure drop of the feed from 2 to 15 bar, for example, from 2.5 to 10 bar, from 3 to 8 bar, from 3 to 10 bar, or from 4 to 9 bar (e.g., from 5 to 8 bar), for example, to manage the amount of pressurization required before the feed enters the thermal energy recovery assembly 30 while promoting a sufficiently high rate of heat transfer from the inner tube to the feed.
  • a pressure drop of the feed from 2 to 15 bar, for example, from 2.5 to 10 bar, from 3 to 8 bar, from 3 to 10 bar, or from 4 to 9 bar (e.g., from 5 to 8 bar), for example, to manage the amount of pressurization required before the feed enters the thermal energy recovery assembly 30 while promoting a sufficiently high rate of heat transfer from the inner tube to the feed.
  • the thermal energy recovery assembly 30 may be configured and/or controlled to quench the hot reactor effluent and to preheat the hydrocarbon feed to a reactor feed temperature.
  • the thermal energy recovery assembly 30 may be configured with one or more stages to transfer heat from the hot reactor effluent to the hydrocarbon feed, which may not be preheated, or at least not preheated sufficiently to supply to a cracking furnace for cracking.
  • the stages may have a tube-in-tube design with the hot reactor effluent flowing through an inner tube and the hydrocarbon feed flowing through an outer tube.
  • the outer tube may include stages having one or more heat transfer enhancements, such as, for example, plate impingement, piccolo impingement, one or more turbulence promoting features associated with the outer tube and/or the inner tube, and/or increased surface area associated with the outer tube and/or the inner tube.
  • the inner tube may include one or more heat transfer enhancements configured to promote heat transfer from the hot reactor effluent. Configuring the one or more stages and inner tube may include selecting stages to achieve desired properties of the hot reactor effluent while transferring heat to the cold feed.
  • stages may be selected to improve or maximize a cooling rate of the hot reactor effluent, to improve or minimize a pressure drop of the hot reactor effluent, to improve or minimize a residence time of the hot reactor effluent, and/or to improve or minimize a pressure drop of the hydrocarbon feed.
  • the thermal energy recovery assembly may include a plurality of inner tubes parallel with one another, with each inner tube disposed within an outer tube and each outer tube having one or more heat transfer enhancements to enhance heat transfer from the inner tube to an annulus defined within the outer tube.
  • the thermal energy recovery assembly may include a plurality of inner tubes parallel with one another, with each inner tube disposed within an outer tube, and with the outer tube and optionally the inner tube having one or more heat transfer enhancements to enhance heat transfer from the inner tube to an annulus defined within the outer tube.
  • FIG. 4A is a schematic section view of an example inner tube 34a including example rounded projections 70a on an interior surface 72a of the inner tube 34a, according to embodiments of the disclosure.
  • the interior surface 72a of the inner tubes 34 may include turbulence-promoting structures and/or structures to increase the surface area of the interior surface 72a.
  • the interior surface 72a of the inner tube 34a may include one or more rounded projections 70a.
  • the one or more rounded projections 70a may extend toward the center of the inner tube 34a and/or may extend longitudinally, partially, intermittently, or fully, along the length of the inner tube 34a.
  • the rounded projections 70a may be the same or differ from one another.
  • the one or more rounded projections 70a may extend helically along the longitudinal length of the inner tube 34a, for example, to promote swirling of the flow through the inner tube 34a.
  • projections on the interior surface of inner tubes 34 may have a non-rounded configuration.
  • FIG. 4B is a schematic section view of another example inner tube 34b including example rectangular projections 70b on an interior surface 72b of the inner tube 34b, according to embodiments of the disclosure.
  • the interior surface of the inner tubes 34 may include a combination of rounded projections and rectangular projections. Other configurations of projections are contemplated.
  • the inner tube 34 may include turbulence promoting structures and/or structures to increase the surface area of an outer surface of the inner tube 34.
  • turbulence promoting structures and/or structures to increase the surface area of the outer surface of the inner tube 34 may include projections at least similar to the above-noted projections on the interior surface of the inner tube 34.
  • structures to increase the surface area of the outer surface of the inner tube 34 may be configured to enhance the effectiveness of the turbulencepromoting structures and/or impingement features.
  • the inner surface of the outer tube 40 may include surface area enhancements, for example, such as those described above. [0057] FIG.
  • FIG. 5 is a block diagram of an example method 500 to heat a hydrocarbon feed including, for example, one or more of ethane, propane, butane, condensate, light naphtha, heavy naphtha, gas oil, pyrolysis oil, materials derived from processing refinery streams, Fischer-Tropsch products, plastic waste, and/or biofeedstocks.
  • the hydrocarbon feed may additionally include steam.
  • the hydrocarbon feed may be preheated and thereafter cracked in an electrically heated cracking furnace, which may output cracked hydrocarbons including olefins.
  • the example method 500 is illustrated in FIG. 5 as a collection of blocks in a logical flow graph, which represent a sequence of operations.
  • any number of the described blocks may be combined in any order and/or in parallel to implement the method.
  • the operations described in one or more of the blocks may be optional and/or omitted from the example method 500, such as, for example, the operations described by blocks 512 and/or 514, although one or more of the operations described by other blocks may also, or alternatively, be omitted from the example method 500.
  • the example method 500 may include supplying a hydrocarbon feed to an outer tube of a thermal energy recovery assembly.
  • the thermal energy recovery system may include any thermal energy recovery systems described herein.
  • the hydrocarbon feed may include, for example, one or more of ethane, propane, butane, condensate, light naphtha, heavy naphtha, gas oil, pyrolysis oil, and/or materials derived from processing refinery streams, Fischer-Tropsch products, plastic waste, or biofeedstocks, or any other hydrocarbons that may be converted to olefins in a cracking process, and may additionally include steam.
  • the hydrocarbon feed may, in some embodiments, include, or be, a hydrocarbon feed supplied by a source of hydrocarbon feed.
  • the example method 500 further may include heating the hydrocarbon feed in the outer tube of the thermal energy recovery assembly to output a preheated hydrocarbon feed.
  • the hydrocarbon feed may be preheated via heat transfer in the thermal energy recovery system with the thermal energy being at least partially supplied by hot reactor effluent of the cracking process.
  • the example method 500, at 506 also may include supplying the preheated hydrocarbon feed to an electrically heated cracking furnace including a reaction zone to heat the preheated hydrocarbon feed, for example, as previously described herein.
  • the example method 500 further may include cracking the preheated hydrocarbon feed in the reaction zone to output hot reactor effluent including cracked hydrocarbons and olefins, for example, as described previously herein.
  • the example method 500, at 510, also may include supplying the hot reactor effluent to an inner tube of the thermal energy recovery assembly, for example, as previously described herein.
  • supplying the hot reactor effluent to the inner tube of the thermal energy recovery assembly may include supplying the hot reactor effluent to the inner tube of the thermal energy recovery assembly at a temperature of at least 350° Celsius, at least 375° Celsius, at least 400° Celsius, at least 425° Celsius, at least 450° Celsius, at least 475° Celsius, at least 500° Celsius, at least 525° Celsius, at least 550° Celsius, at least 575° Celsius, at least 600° Celsius, at least 625° Celsius, at least 650° Celsius, at least 700°C, at least 750°C, at least 800°C, or at least 850°C.
  • the example method 500 further may include supplying additional feed to the outer tube of the thermal energy recovery assembly.
  • the additional feed may, in some embodiments, be a continuation of the supply of hydrocarbon feed at 502 from the hydrocarbon feed source, a different hydrocarbon feed, water, or steam.
  • the additional feed may be supplied to a stage different from the stage to which the hydrocarbon feed is supplied.
  • the additional feed may mix with the hydrocarbon feed, the mixed feed exiting the thermal energy recovery assembly at a common outlet.
  • the additional feed may traverse different stages than does the hydrocarbon feed, and exit through a different outlet.
  • the example method 500 also may include heating the additional feed by transferring heat from the hot reactor effluent to the additional hydrocarbon feed via the thermal energy recovery assembly, for example, as described previously herein.
  • Heating the additional feed in the outer tube of the thermal energy recovery assembly to output a preheated feed may include heating the feed to a temperature of at least 350° Celsius, at least 375° Celsius, at least 400° Celsius, at least 425° Celsius, at least 450° Celsius, at least 475° Celsius, at least 500° Celsius, at least 525° Celsius, at least 550° Celsius, at least 575° Celsius, at least 600° Celsius, at least 625° Celsius, or at least 650° Celsius.
  • supplying the hot reactor effluent to the inner tube of the thermal energy recovery assembly may include quenching the hot reactor effluent via heat transfer to the additional hydrocarbon feed, for example, as described herein.
  • heating the feed in the outer tube of the thermal energy recovery assembly may include preheating the feed via heat transfer to the feed from the hot reactor effluent.
  • the example method 500 may further include enhancing the heat transfer to the additional feed by providing heat transfer enhancements on one or more of the outer tube or the inner tube.
  • the heat transfer enhancements may include one or more of plate impingement, piccolo impingement, turbulence promotion, or increased surface area, for example, as previously described herein.
  • thermal energy recovery assemblies were as follows: (1) a tube-in-tube thermal energy recovery assembly without heat transfer enhancement in an inner tube and with high-shear geometry in an annulus, (2) a thermal energy recovery assembly including fins in the inner tube and turbulence-promoting features in the annulus, (3) a thermal energy recovery assembly including fins in the inner tube and plate impingement in the annulus, (4) a thermal energy recovery assembly including fins in the inner tube and piccolo impingement in the annulus, (5) a thermal energy recovery assembly including a plain tube (no internal fins) and turbulence promoting features in the annulus, (6) a thermal energy recovery assembly including a plain tube and plate impingement in the annulus, and (7) a thermal energy recovery assembly including a plain tube and piccolo impingement in the annulus.
  • boundary conditions for the conventional heat exchanger (“Comp ”) and each of the seven example thermal energy recovery assemblies according to embodiments of the disclosure (1 through 7) were established as follows: hot effluent resulting from steam cracking of ethane was passed through an inner tube, and cold feed including ethane and steam was passed through an outer tube.
  • the hot effluent mass flow rate was 351.6 kilograms/hour, and the outer diameter of the inner tube was 60.3 mm, with a tube wall thickness of 3.6 mm.
  • the hot effluent and the cold feed were flowing according to a counter-current flow with the following inlet and outlet temperatures: Tin, hot equals 827 degrees C; T ou t, hot equals 486 degrees C; Tin, cold equals 236 degrees C; and T ou t, cold equals 650 degrees C.
  • thermal energy recovery assemblies may provide improved performance, for example, in terms of cooling rate, residence time, effluent pressure drop, and/or required cooling surface area as compared to a heat exchanger without such heat transfer enhancement features.
  • higher values of the cooling rate and lower values of the required surface area, the effluent pressure drop, and the effluent residence time may be generally favorable in terms of process performance and/or equipment cost.
  • Heating and cooling profiles for a furnace mixed feed i.e., steam plus naphtha
  • 876.8 tons/hour (t/h) and the reaction zone effluent stream (876.8 t/h) were generated using a process simulation software tool, along with the energy requirement of the steam cracking reaction.
  • Feasible energy balances with and without using a thermal energy recovery assembly were constructed.
  • unit operations downstream of a cracker have a net heat input demand of 163 Megawatts (MW).
  • MW Megawatts
  • Example 2(a) is a comparative example where 120 bar steam is generated in a conventional transfer line exchanger (TLE).
  • the mixed feed temperature is initially at 180 degrees C because available heat recovery from the downstream of the plant can provide this starting temperature.
  • the mixed feed may be heated from 180 degrees C to 300 degrees C using the 120 bar steam, since the saturated steam temperature is 324 degrees C.
  • the remaining steam which constitutes 244 MW of the 314 MW of heat removed from the TLE, is used to supply the 163 MW of downstream heating duty and for 33 MW of mechanical work (i.e., calculated as follows: (244 MW - 163 MW) multiplied by 0.41, which equals 33 MW); the remaining 118 MW of work is supplied by 124 MW of electricity (i.e., calculated as follows: 118 divided by 0.95 equals 124 MW).
  • this comparative Example 2(a) there is no direct feed-effluent heat exchange. The feed is heated from 300 degrees C to 650 degrees C electrically, and the cracking reaction is driven by electric heating.
  • 682 MW of electricity is needed for preheating in addition to the reaction, resulting in a total electricity usage in this comparative example of 806 MW.
  • Example 2(b) an example according to embodiments of the disclosure, the mixed feed is preheated to 450 degrees C by feed-effluent heat exchange using a thermal energy recovery assembly according to embodiments of the disclosure.
  • the remaining cooling of the cracked gas is achieved by steam generation, recovering 145 MW, which may provide the energy for all but 18 MW of the downstream heating; all of the mechanical work may be performed electrically, which requires 159 MW of electricity according to this example.
  • the feed is heated from 450 degrees C to 650 degrees C electrically, and the cracking reaction is driven by electric heating.
  • the total electricity needed for the feed in addition to the furnace heating in this example is 583 MW, resulting in a total electricity usage of 760 MW.
  • Example 2(c) a further example according to embodiments of the disclosure, the mixed feed may be heated to the relatively higher temperature of 550 degrees C using the thermal energy recovery assembly according to embodiments of the disclosure.
  • the thermal energy recovery assembly As the amount of heat transferred from the thermal energy recovery assembly to the feed is increased, the amount of steam generation decreases, and the amount of electricity required for the feed and cracking reaction decreases.
  • the feed is heated from 550 degrees C to 650 degrees C electrically, and the cracking reaction is driven by electric heating.
  • 72 MW of steam are generated, which may be used to supply some of the downstream heating; all of the mechanical work may be performed done electrically.
  • the total electricity needed for the feed in addition to the furnace heating in this example is 511 MW, resulting in a total electricity usage of 760 MW.
  • Example 2(d) another example according to embodiments of the disclosure, the feed preheat is increased to 650°C and the steam generation is eliminated. A small adjustment to the hot side target temperature down from 400 degrees C to 392 degrees C marks the enthalpy balance point with this feed and target preheating condition.
  • 433 MW of electricity is required at the furnace. No steam is generated, so 163 MW of electricity are required for the downstream heating, and 159 MW of electricity are required for the mechanical work, resulting in a total electricity consumption of 755 MW.
  • Example 2(e) yet a further example according to embodiments of the disclosure, steam generation is employed only to the extent that the steam is used for mixed feed preheating to 300 degrees C; the remainder of the preheating is achieved using a tube-in-tube exchanger according to embodiments of the disclosure. There is no steam export.
  • the total electric heating duty at the furnace is 433 MW, which is the same as for Example 2(d)), and 250 MW less than the comparative example (i.e., Example 2(a)).
  • Example 2(e) 163 MW of electricity are required for the downstream heating, and 159 MW of electricity are required for the mechanical work, resulting in a total electricity consumption of 755 MW, or 51 MW less than in the comparative example (i.e., Example 2(a)).
  • Example 2(a) through 2(e) A summary of the heat and electricity usage for Examples 2(a) through 2(e) is provided in TABLE B below. Comparing the comparative Example 2(a) with Examples 2(b) through 2(e), examples according to embodiments of the disclosure, shows that the total amount of electricity required to operate the cracking process is reduced when the feed is preheated to a temperature of at least 450°C using example thermal energy recovery assemblies according to embodiments of the disclosure. This demonstrates that thermal energy recovery assemblies consistent with embodiments of the disclosure may promote an increased efficiency, for example, when a sufficiently high level of preheat is achieved. Among Examples 2(b) through 2(e), the electricity requirement may remain essentially the same, showing that thermal energy recovery assemblies consistent with embodiments of the disclosure may be used flexibly without loss of efficiency, for example, as long as a minimum level of preheat is accomplished.
  • Examples 3(a) through 3(e) are analogous to Examples 2(a) through 2(e) above, except that the order of heat exchange is reversed on the hot cracked gas cooling stream. Steam generation is used for the first part of the cooling and feed-effluent heat exchange is used for the secondary cooling.
  • a summary of the results of Examples 3(a) through 3(e) is given in TABLE C below. As with Examples 2(a) through 2(e), the results show the total electricity consumed by the cracking process may be decreased through the use of thermal energy recovery assemblies consistent with embodiments of the disclosure.
  • An example thermal energy recovery assembly A to recover thermal energy from hot reactor effluent to heat a feed to an electrically powered reactor furnace may include an inner tube having a first inlet configured to receive hot reactor effluent from an electrically powered reactor furnace, and an outer tube disposed about the inner tube to enclose an annulus about the inner tube.
  • the annulus may have a second inlet configured to receive a feed to the electrically powered reactor furnace, and the annulus may be configured to use the feed for the electrically powered reactor furnace as a cooling medium to recover thermal energy from the hot reactor effluent prior to the feed being supplied to the electrically powered reactor furnace.
  • the annulus may be configured to enhance heat transfer from the hot reactor effluent to the feed in the annulus.
  • hot reactor effluent may reach a first inlet via a gas inlet chamber or other connector.
  • cooling may be supplied to the gas inlet chamber or other connector.
  • the gas chamber may connect one or more than one cracking coil to one or more than one inner tube.
  • a header may be provided to connect the feed to more than one annulus.
  • cooled cracked gas from more than one inner tube may be collected using a header.
  • heated feed from more than one annulus may be combined via a header.
  • multiple annuli may be contained in a single mechanical device, which may receive hot effluent from multiple cracking coils via a gas inlet chamber or other connector, and cold feed from a feed header.
  • the outer tube includes a first stage
  • the at least one heat transfer enhancement comprises one or more of a plate impingement, a piccolo impingement, turbulence promotion, or increased surface area.
  • heat transfer enhancement by impingement may refer to flow of fluid passing through the outer tube, whose average direction as it proceeds from inlet to outlet may be substantially parallel to the inner tube, being purposely directed to flow toward the inner tube, for example, using geometric features introduced into the annulus.
  • this directed (impinging) flow may, for example, be perpendicular to the inner tube, or directed toward the inner tube at an angle greater than thirty degrees relative to an axis of the inner tube, while its velocity may be relatively greater than a superficial velocity of the outer-tube fluid (for example, the volumetric flow of the outer-tube fluid divided by the area of the annular cross-section between the inner and outer tube).
  • the geometric features that promote impingement may include, for example, nozzles and/or openings oriented toward the inner tube, and/or obstructions placed in a flow path that may redirect fluid from a direction that is more parallel to the inner tube more directly towards the outer surface of the inner tube.
  • These example features may be implemented in a periodic fashion, for example, resulting in impingement zones that occur at intervals along the length and/or the circumference of the inner tube. Applicant has discovered that introduction of such impingement features may increase the rate of heat transfer relative to the rate that would be attained by parallel flow through the outer tube.
  • a ratio of a velocity of an impinging flow to the superficial velocity may be greater than two, greater than five, or greater than ten.
  • the velocity of the impinging flow may be approximated, in the case of nozzles or openings, as the volumetric flow divided by the total flow area defined by the nozzles or openings, through which the flow is directed.
  • the heat transfer enhancement may be found to be more suitable at distances between the impingement-inducing feature (e.g., between nozzles or openings 54) and the inner tube that are from about the diameter to about twelve times the diameter of the nozzles or openings 54, or from about the diameter to about ten times the diameter, or from about two times the diameter to about eight times the diameter.
  • impingement features may include plate impingement and/or piccolo impingement.
  • the outer tube includes a plate impingement disposed between an upstream end and a downstream end.
  • the plate impingement may include a first channel having a stage inlet at the upstream end being closed to flow at the downstream end.
  • the plate impingement also may include a second channel having a stage outlet at the downstream end.
  • the second channel may be disposed between the first channel and the inner tube.
  • the plate impingement may further include a wall separating the first channel from the second channel.
  • the wall may define openings to fluidly connect the first channel and the second channel.
  • the plate impingement may be configured to receive feed through the stage inlet, flow feed from the first channel to the second channel via the openings of the wall to impinge onto an outer surface of the inner tube, and exhaust feed through the stage outlet of the second channel.
  • the piccolo impingement may include an upstream divider disposed about the inner tube and within the outer tube, a downstream divider disposed about the inner tube and within the outer tube downstream of the upstream divider within annulus.
  • the downstream divider may define at least one stage outlet.
  • the piccolo impingement also may include a chamber defined within the outer tube and about the inner tube between the upstream divider and the downstream divider, and piccolo tubes parallel to or at an angle with respect to the inner tube, and/or may be straight, curved, or bent, and/or offset from the inner tube.
  • the piccolo tubes may extend through the chamber from the upstream divider to the downstream divider.
  • the piccolo tubes may include a stage inlet for receiving incoming feed, and a plurality of openings defined therein, and the openings may be oriented toward the outer surface of the inner tube.
  • the piccolo impingement may be configured to receive feed from the stage inlets, flow feed from the piccolo tubes into the chamber via the plurality of openings, impinge the flow onto the outer surface of the inner tube, and/or exhaust feed from the chamber via the at least one stage outlet.
  • the at least one stage includes a first stage and a second stage; and one or more of: (1) the inner tube of the first stage has a first outlet and is configured to flow hot reactor effluent from the first inlet to the first outlet, the outer tube of the first stage has a second outlet and is configured to flow feed from the second inlet to the second outlet, and the second inlet of the first stage is adjacent the first outlet of the first stage and the second outlet of the first stage is adjacent the first inlet of the first stage; (2) the second stage includes at least one heat transfer enhancement including one or more of a plate impingement, a piccolo impingent, turbulence promotion, or increased surface area, the second stage being in series with the first stage; or (3) the second stage including an inner tube having a first inlet and a first outlet and is configured to flow reactor effluent from the first inlet of the second stage to the first outlet of the second stage; an outer tube having a second inlet and a second outlet and is configured to flow feed
  • the inner tube has a first outlet and configured to flow hot reactor effluent from the first inlet to the first outlet
  • the outer tube having a second outlet and configured to flow feed from the second inlet to the second outlet, and one of: the second inlet is adj acent the first outlet and the second outlet is adj acent the first inlet; or the first inlet is adj acent second inlet and the first outlet is adjacent the second outlet.
  • the thermal energy recovery assembly includes a plurality of inner tubes parallel with one another with each inner tube disposed within an outer tube, each outer tube having one or more at least one of a plate impingement, a piccolo impingement, or turbulence promotion to enhance heat transfer from the inner tube to an annulus defined within the outer tube.
  • the thermal energy recovery assembly may include a plurality of inner tubes parallel with one another, with each inner tube disposed within an outer tube, and with the outer tube and optionally the inner tube having one or more heat transfer enhancements to enhance heat transfer from the inner tube to an annulus defined within the outer tube.
  • the thermal energy recovery assembly is configured: to cool the hot reactor effluent at a rate of at least 2.5 degrees Kelvin/millisecond, at least 3.5 degrees Kelvin/millisecond, at least 4.5 degrees Kelvin/millisecond, at least 5 degrees Kelvin/ms, or at least 5.5 degrees Kelvin/ms, for example, where the cooling rate may be defined as the inlet temperature of the hot reactor effluent (in degrees K) minus 923 K, divided by the residence time required for cooling from the temperature of the hot reactor effluent to 923 K, unless the inlet temperature of the hot reactor effluent (in degrees K) is less than 923 K or the temperature of the cooled reactor effluent is greater than 923K, in which case the cooling rate may be defined as the inlet temperature of the hot reactor effluent (in degrees K) minus the temperature of the cooled reactor effluent when it leaves the thermal energy recovery assembly, divided by the residence time of the effluent in the
  • the thermal energy recovery assembly may be configured such that a pressure drop of the hot reactor effluent passing through the thermal energy recovery assembly is less than 0.35 bar, less than 0.30 bar, less than 0.25 bar, or less than 0.20 bar; such that a residence time of the hot reactor effluent within the thermal energy recovery assembly is less than 100 milliseconds, less than 95 milliseconds, less than 90 milliseconds, less than 85 milliseconds, is less than 83 milliseconds, or is less than 80 milliseconds; or such that a pressure drop of the feed passing through the thermal energy recovery assembly is less than 15 bar, less than 12 bar, less than 10 bar, less than 8 bar, or less than 6 bar.
  • thermal energy recovery assembly configured to preheat the feed to at least 350° Celsius, at least 375° Celsius, at least 400° Celsius, at least 425° Celsius, at least 450° Celsius, at least 475° Celsius, at least 500° Celsius, at least 525° Celsius, at least 550° Celsius, at least 575° Celsius, at least 600° Celsius, at least 625° Celsius, or at least 650° Celsius.
  • a furnace assembly for heating a feed to provide a hot reactor effluent may include the example thermal energy recovery assembly A above; and an electrically powered reactor furnace including a reaction zone configured to heat a feed to a cracking temperature thereof of one or more of ethane, propane, butane, condensate, light naphtha, heavy naphtha, gas oil, pyrolysis oil, materials derived from processing refinery streams, Fischer-Tropsch products, plastic waste, or biofeedstocks.
  • a method B to produce olefins may include supplying a hydrocarbon feed to an outer tube of a thermal energy recovery assembly, and heating the hydrocarbon feed in the outer tube of the thermal energy recovery assembly to output a preheated hydrocarbon feed.
  • the example method B also may include supplying the preheated hydrocarbon feed to an electrically heated cracking furnace comprising a reaction zone to heat the preheated hydrocarbon feed, and cracking the preheated hydrocarbon feed in the reaction zone to output hot reactor effluent comprising cracked hydrocarbons and olefins.
  • the example method B further may include supplying the hot reactor effluent to an inner tube of the thermal energy recovery assembly, and supplying additional hydrocarbon feed to the outer tube of the thermal energy recovery assembly.
  • the example method B also may include heating the additional hydrocarbon feed by transferring heat from the hot reactor effluent to the additional hydrocarbon feed via the thermal energy recovery assembly.
  • the example method B above wherein one or more of: (1) supplying the hot reactor effluent to the inner tube of the thermal energy recovery assembly includes quenching the hot reactor effluent via heat transfer to the additional hydrocarbon feed; or (2) heating the hydrocarbon feed in the outer tube of the thermal energy recovery assembly comprises preheating the hydrocarbon feed via heat transfer to the hydrocarbon feed from the hot reactor effluent.
  • the example method B above further including enhancing the heat transfer to the additional hydrocarbon feed by providing heat transfer enhancements on one or more of the outer tube or the inner tube, the heat transfer enhancements including one or more of plate impingement, piccolo impingement, or turbulence promotion.
  • supplying the hot reactor effluent to the inner tube of the thermal energy recovery assembly includes supplying the hot reactor effluent to the inner tube of the thermal energy recovery assembly at a temperature of at least 350° Celsius, at least 375° Celsius, at least 400° Celsius, at least 425° Celsius, at least 450° Celsius, at least 475° Celsius, at least 500° Celsius, at least 525° Celsius, at least 550° Celsius, at least 575° Celsius, at least 600° Celsius, at least 625° Celsius, or at least 650° Celsius.
  • heating the hydrocarbon feed in the outer tube of the thermal energy recovery assembly to output a preheated hydrocarbon feed comprises heating the hydrocarbon feed to a temperature of at least 350° Celsius, at least 375° Celsius, at least 400° Celsius, at least 425° Celsius, at least 450° Celsius, at least 475° Celsius, at least 500° Celsius, at least 525° Celsius, at least 550° Celsius, at least 575° Celsius, at least 600° Celsius, at least 625° Celsius, or at least 650° Celsius.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Geometry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé de production d'oléfines qui peut consister à fournir une charge d'hydrocarbures à un tube externe d'un ensemble de récupération d'énergie thermique ; chauffer la charge d'hydrocarbures dans le tube externe de l'ensemble de récupération d'énergie thermique pour délivrer en sortie une charge d'hydrocarbures préchauffée ; fournir la charge d'hydrocarbures préchauffée à un four de craquage à alimentation électrique comprenant une zone de réaction pour chauffer la charge d'hydrocarbures préchauffée ; craquer la charge d'hydrocarbures préchauffée dans la zone de réaction du four de craquage chauffé électriquement à l'aide de la chaleur générée par l'électricité pour produire un effluent de réacteur chaud comprenant des hydrocarbures et des oléfines craqués ; fournir l'effluent de réacteur chaud à un tube interne de l'ensemble de récupération d'énergie thermique ; et refroidir l'effluent de réacteur chaud dans le tube interne de l'ensemble de récupération d'énergie thermique par transfert de chaleur vers la charge d'hydrocarbures.
PCT/EP2022/073363 2021-08-27 2022-08-22 Appareil de craquage chauffé électriquement et dispositif de récupération d'énergie thermique WO2023025737A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP21193413.8 2021-08-27
EP21193413 2021-08-27

Publications (1)

Publication Number Publication Date
WO2023025737A1 true WO2023025737A1 (fr) 2023-03-02

Family

ID=77520523

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2022/073363 WO2023025737A1 (fr) 2021-08-27 2022-08-22 Appareil de craquage chauffé électriquement et dispositif de récupération d'énergie thermique

Country Status (1)

Country Link
WO (1) WO2023025737A1 (fr)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB969036A (en) * 1960-09-21 1964-09-09 Fives Penhoet Improvements in or relating to tubular heat exchange apparatus
US5295822A (en) * 1991-05-03 1994-03-22 Indugas, Inc. Convective heat transfer by cascading jet impingement in a batch coil annealling furnace
FR2831154A1 (fr) * 2001-10-18 2003-04-25 Physiques Ecp Et Chimiques Assistance electrique au reformage d'une matiere hydrocarbonee
RU2663370C1 (ru) * 2017-07-25 2018-08-03 Федеральное государственное бюджетное образовательное учреждение высшего образования "Калининградский государственный технический университет" Теплообменник
EP3725865A1 (fr) * 2019-04-17 2020-10-21 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
EP3895795A1 (fr) * 2020-04-18 2021-10-20 Gianluca Pauletto Réacteur comportant un catalyseur de céramique structuré chauffé électriquement
WO2022094455A1 (fr) * 2020-11-02 2022-05-05 Lummus Technology Llc Four électrique pour la production d'oléfines

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB969036A (en) * 1960-09-21 1964-09-09 Fives Penhoet Improvements in or relating to tubular heat exchange apparatus
US5295822A (en) * 1991-05-03 1994-03-22 Indugas, Inc. Convective heat transfer by cascading jet impingement in a batch coil annealling furnace
FR2831154A1 (fr) * 2001-10-18 2003-04-25 Physiques Ecp Et Chimiques Assistance electrique au reformage d'une matiere hydrocarbonee
RU2663370C1 (ru) * 2017-07-25 2018-08-03 Федеральное государственное бюджетное образовательное учреждение высшего образования "Калининградский государственный технический университет" Теплообменник
EP3725865A1 (fr) * 2019-04-17 2020-10-21 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
EP3895795A1 (fr) * 2020-04-18 2021-10-20 Gianluca Pauletto Réacteur comportant un catalyseur de céramique structuré chauffé électriquement
WO2022094455A1 (fr) * 2020-11-02 2022-05-05 Lummus Technology Llc Four électrique pour la production d'oléfines

Similar Documents

Publication Publication Date Title
Amghizar et al. Sustainable innovations in steam cracking: CO 2 neutral olefin production
US4361478A (en) Method of preheating hydrocarbons for thermal cracking
RU2405622C2 (ru) Лопаточный реактор для пиролиза углеводородов
US7232937B2 (en) Process for producing low-molecular olefins by pyrolysis of hydrocarbons
US5324486A (en) Hydrocarbon cracking apparatus
US5092981A (en) Process for quenching hydrocarbon cracking apparatus effluent
EP0245839B1 (fr) Procédé de pyrolyse pour charges flexibles
WO2023025737A1 (fr) Appareil de craquage chauffé électriquement et dispositif de récupération d'énergie thermique
US20230407186A1 (en) Electric furnace to produce olefins
EP3443053B1 (fr) Réacteur pour un four de craquage
CN118139949A (zh) 用于电热裂解过程的热能回收装置
EP2248581A1 (fr) Processus de refroidissement des gaz émis d'un four
CN111826173B (zh) 用于制备低碳烯烃的反应装置、生产系统和生产方法
US20120203049A1 (en) Heat exchange device and a method of manufacturing the same
KR20230050365A (ko) 셸 앤드 튜브 열 교환기, 열 교환 방법 및 열 교환기의 사용
US20120060727A1 (en) Process for quenching the effluent gas of a furnace
US11618857B1 (en) Electric furnace for cracking hydrocarbon feedstock with heat recovery
EP2230009A1 (fr) Processus de refroidissement des gaz émis d'un four
CN201473469U (zh) 两程式和多程式锥形炉管的裂解炉
TW202344778A (zh) 外部燃燒空氣預熱
WO2023114623A1 (fr) Système et procédé de récupération de service pour four de vapocraquage
CN110184086A (zh) 用于轻烃热裂解的裂解炉
CN118076431A (zh) 利用旋转产生的热能在与精炼和石化工业相关的过程中加热流体的方法和设备
Plumley et al. 4785622 Integrated coal gasification plant and combined cycle system with air bleed and steam injection

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 22768398

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 2024103403

Country of ref document: RU

WWE Wipo information: entry into national phase

Ref document number: 2022768398

Country of ref document: EP

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2022768398

Country of ref document: EP

Effective date: 20240327