EP0205205A1 - Refroidisseur de conduit de transfert - Google Patents

Refroidisseur de conduit de transfert Download PDF

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Publication number
EP0205205A1
EP0205205A1 EP86200931A EP86200931A EP0205205A1 EP 0205205 A1 EP0205205 A1 EP 0205205A1 EP 86200931 A EP86200931 A EP 86200931A EP 86200931 A EP86200931 A EP 86200931A EP 0205205 A1 EP0205205 A1 EP 0205205A1
Authority
EP
European Patent Office
Prior art keywords
tube
transfer
tubes
heat exchanging
cooling
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP86200931A
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German (de)
English (en)
Inventor
Jelle Douwe Homans
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Dow Chemical Nederland BV
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Dow Chemical Nederland BV
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Filing date
Publication date
Application filed by Dow Chemical Nederland BV filed Critical Dow Chemical Nederland BV
Publication of EP0205205A1 publication Critical patent/EP0205205A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • F28F9/26—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators
    • 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
    • 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
    • F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
    • F28D7/0083—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium
    • F28D7/0091—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium the supplementary medium flowing in series through the units
    • 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
    • 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
    • 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
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0075—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for syngas or cracked gas cooling systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F2265/00—Safety or protection arrangements; Arrangements for preventing malfunction
    • F28F2265/26—Safety or protection arrangements; Arrangements for preventing malfunction for allowing differential expansion between elements

Definitions

  • the present invention relates to a transfer-line cooler, and, more particularly, to a transfer-line cooler having two separate heat exchanging sections.
  • the cracking reaction is normally conducted at cracking temperatures between 700°C and 1100°C.
  • LPG liquid propane gas
  • the cracking reaction is normally conducted at cracking temperatures between 700°C and 1100°C.
  • the desired cracking reactions have occured, to reduce the formation of undesirable by-products caused by additional cracking, it is desirable to cool the cracked reaction product to a sufficiently low temperature such that the cracking reactions are terminated or reduced to a desirable rate.
  • the temperature required for this purpose is generally between 500° and 700°C.
  • the reaction product is cooled to a temperature sufficiently low to terminate the cracking-reactions, theoactual temperature to which the reaction product-is cooled is not critical.
  • the critical feature is the time required- to sufficiently reduce the temperature, with the shortest time possible being preferred.
  • the cracked reaction product is advantageously cooled to the indicated temperatures in less than 0.1 second.
  • a transfer-line exchanger is a shell and tube type heat exchanger wherein the cracked reaction product flows through a distribution header into and through a plurality of tubes to a collection header at the opposite end. At each end, the tubes extend through and are welded to a tube sheet.
  • the cooling medium commonly water or a water/steam mixture
  • the shell section i.e., on the outside of the tubes, usually in a cocurrent flow to the cracked reaction product.
  • a heat exchanger of particular interest for use as a transfer-tine exchanger is a double tube type heat exchanger described in "Recuperacion de Calor en Grandes Unidades Quimicas y Petroquimicas" by Hellmut Hermann, Ingeniera Quimica, May 1984 pps. 71-84.
  • an inner tube or conduit for carrying the cracked hydrocarbon reaction product is enclosed by a large diameter tube or . conduit for carrying the cooling fluid.
  • a sufficiently large transfer-line exchanger to cool the-.cracked reaction product at a desired rate is employed to terminate the cracking reactions.
  • the cracked reaction product is further cooled by quenching the reaction product such as by the direct addition of a hydrocarbon oil.
  • conservation of energy and/or heat is always desired.
  • the use of a single transfer line exchanger followed by a quench in the cooling of the cracked reaction product is not particularly effectively in producing heat and/or energy.
  • two transfer-line exchangers -a primary transfer-line exchanger ("PTLE") and secondary transfer-line exchanger ("STLE”) -are employed to cool the cracked reaction product.
  • the cracked reaction product flows sequentially through the PTLE and then the STLE, with the cracked gas collection header ("topcone") of the primary transfer-line exchanger being in fluid communication with the inlet or distribution header - ("undercone") of the secondary transfer-line exchanger.
  • the cracked reaction product is cooled to a sufficiently low temperature to stop or reduce the cracking reactions to a desirable slow rate.
  • the water generally employed as a cooling medium in the PTLE is converted to a water/steam mixture at a high pressure.
  • This generated water/steam mixture can subsequently be used to generate high pressure steam for use as a source of energy and/or heat.
  • the cracked reaction product is further cooled.
  • the water employed as a cooling medium in the STLE is converted to a water/steam mixture at low pressures.
  • the present invention is a transfer-line exchanger and a method for cooling of a fluid such as a cracked reaction product which reduces the pressure loss caused by the cooling operation and permits the effective use of the cooling media as a source of heat and/or energy.
  • the transfer-line exchanger of the present invention is a shell and tube type heat exchanger having two or more separate heat exchanging sections but only one inlet and one collection header, the separate sections being joined by intermediate tubes.
  • the present invention is an improved transfer-line cooler which comprises two shell and tube heat exchange sections each having tube(s), tube sheets and shells, wherein the tube-(s) of the first heat exchanger communicate a high temperature fluid being cooled to corresponding tube(s) in the second heat exchange section through intermediate tube(s), wherein the improvement comprises the intermediate tubes being positioned loosely in gude sleeves, the intermediate tubes being contained within a tight compartment.
  • the guide sleeves are located .on the tube sheets at the nearest ends of the shells of the two heat exchanger sections.
  • Such a transfer line exchanger typically comprises an inlet header,..a - collection header and two heat exchanging sections.
  • the inlet and collection headers are in fluid communication with each other by means of the tube or plurality of tubes (i.e., a tube bundle) for carrying the higher temperature fluid.
  • Each tube passes through its heat exchanging zone and is open at its two ends.
  • Each end of each tube is secured to a tube sheet.
  • the tube sheet and tube(s) are in fluid communication with the inlet header.
  • the tube end is secured to a second tube sheet in fluid communication with the collection header.
  • the first heat exchanging zone of the heat exchanging section comprises an inlet and an outlet for a first cooling medium and a defined space for the passage of the first cooling medium through the first heat exchanging zone such that the cooling medium contacts at least a portion of the length of the tube or tube bundle containing the higher temperature fluid extending through the first heat exchanging zone.
  • the second heat exchanging zone comprises an inlet and an outlet for a second cooling medium and a defined space therein for the passage of the second cooling medium from the second inlet to the second outlet such that the second cooling medium contacts a portion of the tube or tube bundles containing the high temperature fluid extending through the second heat exchanging zone.
  • a third or "dummy" tube which is not mechanically bonded to either tube portion is positioned in guide sleeves between the first and second tube exchanging zones and provides fluid communication between the first and second tube portions.
  • the present invention is an improved process for cooling a cracked reaction product from a cracking furnace which comprises supplying the cracked reaction product to a two stage transfer-line cooler which comprises two shell and tube heat exchange sections each having tube-(s), tube sheets and shells, wherein the tube(s) of the first heat exchange section communicate the high temperature cracked reaction product being cooled to corresponding tube(s) in the second heat exchange section through intermediate tubes.
  • the intermediate tubes are positioned loosely in guide sleeves which are located on the tube sheets at the nearest ends of the shells of the two heat exchange sections and the intermediate tubes are contained within a tight compartment.
  • reaction product of a hydrocarbon cracker flowing through the tube or tube bundle is sequentially cooled by a first cooling medium at a first temperature flowing around the first heat exchanging zone or compartment and then with a second cooling fluid at a second temperature which is-tes& than the temperature of the first cooling fluid flowing around the second portion, of the tube or tube bundle in the second heat exchanging zone or compartment.
  • the temperature of a fluid can quickly and effectively be reduced to a lower temperature.
  • the efficiency of the heat exchanging operation is effectively increased by sequentially cooling the high temperature fluid using two or more cooling fluids having different temperatures.
  • the steam or water/steam mixture-(s) having a desired temperature and pressure can be generated in the first and second heat exchanging zones or compartments. In such manner, the overall energy efficiency of the system using the described transfer-line exchanger can be improved.
  • the pressure loss in the transfer-line exchanger of the present invention is significantly less than that exhibited using the combination of primary and secondary transfer-line exchangers. Both cocurrent and countercurrent operations are possible using the transfer-line exchanger of the present invention.
  • the exchanger can be employed vertically, horizontally or even at an angle.
  • a single transfer-line exchanger having two separate heat exchanging zones can effectively be employed in various cooling operations, including the cooling of a cracked reaction product exiting from a cracking furnace.
  • the transfer-line exchanger of the present invention can be employed to cool the cracked reaction product to the same or lower temperature using significantly less physical space and capital expenditure than a combination of a primary transfer-line exchanger followed by a secondary transfer-line exchanger.
  • the illustrated transfer-line exchanger consists of a first heat exchanging zone or compartment 20 and a second heat exchanging zone or compartment 30 separated by zone 10 in Figure 1.
  • the transfer-line exchanger further comprises an inlet or distribution header or chamber 29 and an outlet or collection header or chamber 39.
  • Extending from a first tube sheet 23 through the first heat exchanging zone or compartment 20 to a second tube sheet 23a and then from a first tube sheet 33 through the second heat exchanging zone or compartment 30 and to a second tube sheet 33a are a plurality of conduits (e.g., tubes) 24.
  • the plurality of conduits or tubes 24 is commonly referred to as a tube bundle.
  • the conduits 24 are secured, generally by welding or brazing, to he tube sheets.
  • the tube sheets 23 and 33a are depicted as flat plates in the illustrated embodiment, the distribution and collection head- srs 29 and 39, respectively, can comprise a variety 3 f different shapes. Specifically, cylindrical distribu- ion and collection headers such as described in J.S. Patent No. 4 191 247; 4 163 473 and 4 336 342 can be employed. Alternatively, a spherical jistribution or collection chamber can also be em- J loyed.
  • the conduits are open at both ends and are in fluid communication with an inlet conduit 22 via the distribution header 29 and in fluid communication with an outlet conduit 32 via the collection header 39.
  • the conduits 24 are shown to occupy J nly a part of the heat exchanging zones or com- 3 artments 20 and 30. In the actual fabrication of the transfer-line exchanger, conduits 24 will occupy much of the cross-sectional area defined within the heat exchanging zones or compartments.
  • the conduits 24 extending through the first and second heat exchanging zones or compartments are supported by some adequate means - (not shown) at various points throughout the zones or compartments. Such means are well-known in the art and reference is made thereto for the purposes of this invention.
  • the actual heat transfer is conducted in the first and second heat exchanging zones or compartments 20 and 30.
  • the first heat exchanging zone the higher temperature fluid is initially cooled to a lower temperature.
  • the first zone 20 is defined by the housing or shell 21 and the tube sheets 23 and 23a.
  • Conduits 25 and 26 are provided in zone 20 for the introduction and removal of the first cooling fluid from the heat exchanging zone or compartment 20. Whether conduit 25 or 26 is an inlet or an outlet for the first cooling fluid is dependent on the type of operation, i.e., whether the heat exchanger is employed in a cocurrent or countercurrent type operation. For example, in countercurrent operation conduit 26 will act as an inlet and conduit 25 as an outlet for the cooling fluid.
  • the transfer-line exchanger is normally more advantageously operated cocurrently.
  • the conduit 25 acts as an inlet for the first cooling fluid and conduit 26 as an outlet for this fluid.
  • the narrow spaces 27 defined by adjacent conduits 24 and the shell 21 provide for the passage of the first cooling fluid through the first heat exchanging zone or compartment of the transfer-line exchanger and the required contact between the first cooling fluid and the tubes or conduits carrying the higher temperature fluid.
  • the second heat exchanging zone or compartment 30 comprises that zone of the transfer-line exchanger wherein the partially cooled fluid running through tubes 24 is further cooled with a second cooling fluid.
  • the second cooling fluid is of a lower temperature than the cooling fluid used in the first heat exchanging zone or compartment 20.
  • the second heat exchanging zone or compartment 30 is defined by shell 31 and tube sheets 33 and 33a.
  • Conduits 35 and 36 are provided for the introduction and removal of the second cooling fluid to and from the heat exchanging zone or compartment 30.
  • conduit 35 acts as an inlet for the second cooling fluid
  • conduit 36 acts as an outlet.
  • the space is defined by adjacent conduits 24 and the shell 31 provides for the passage of the second cooling fluid through the second heat exchanging zone or compartment 30 of the transfer-line exchanger and the required contact between the second cooling fluid and the tubes carrying the partially cooled, higher temperature fluid.
  • the tubes 24 carry the higher temperature fluid and the shell portions of heat exchanging zones 20 and 30 carry the lower temperature fluids. In this manner, the fluid flowing through the tubes is cooled by-the transfer of heat through the tube to the lower temperature fluid flowing through the shell of the transfer-line exchanger.
  • the heat exchange operation in either or both the heat exchanging zones, can be conducted using cocurrent or countercurrent techniques.
  • cocurrent techniques are most advantageously employed in both heat exchanging zones or compartments and, for purposes of illustration, the operation of the transfer-line exchanger depicted in Fig. 1 will be described with reference to cocurrent heat exchange operation.
  • the higher temperature fluid such as the cracked reaction product is flowed from inlet 22 into the distribution or inlet header 29.
  • the flow of this higher temperature fluid is indicated by the arrow identified by numeral 61.
  • the higher temperature fluid flows, as indicated by the arrows 62, from distribution header 29 into the conduits 24 and, via conduits 24, through the heat exchanging zones 20 and 30.
  • a first cooling (i.e., lower temperature) fluid is conducted, as indicated by the arrows identified by numerals. 63 and 64, via inlet conduit 25 into the space 27 defined by adjacent conduits 24 and conduits 24 and shell 21.
  • the lower temperature fluid flows through the space 27 cocurrently with the flow of the higher temperature fluid through the conduits 24.
  • the higher temperature fluid is cooled as it flows through conduits 24 by the lower temperature fluid flowing through space 27.
  • the lower temperature fluid flows from the first heat exchanging zone 20, as indicated by the arrows identified as 65 and 66, via outlet conduit 26.
  • the partially cooled, high temperature fluid is flowed from the first heat exchanging zone 20 into the second heat exchanging zone 30.
  • a second cooling fluid generally at a lower temperature than the first cooling fluid, is flowed, as indicated by the arrows identified by numeral 67, via inlet conduit 35, into the heat exchanging zone 30 and through space 37 defined by adjacent conduits 24 and conduits 24 and shell 31, as indicated by the arrow identified by numeral 68, cocurrently with the flow of the high temperature fluid through the conduits 24.
  • the high temperature fluid is further cooled by the lower temperature cooling fluid flowing through space 37.
  • the second cooling fluid flows, as indicated by arrows identified by the numerals 69 and 70, from the second heat exchanging zone via outlet conduit 36. As indicated by the arrows identified by numerals 71 and 72, -the now cooled high- temperature fluid is flowed from conduits 24 to the collection header 39 and from the collection header 39 from the transfer-line - exchanger via-outlet conduit 32.
  • the cooling i.e., lower temperature fluid
  • water or a water/steam mixture is advantageously employed as the cooling fluid for cooling the high temperature, cracked reaction product and the water in the cooling fluid is vaporized to form steam during the heat exchanging operation.
  • high pressure steam e.g., steam having a pressure of from 40 to 120 bar
  • water at its boiling temperature and pressure as the cooling fluid in that zone.
  • the partially cooled, cracked reaction product, having a temperature from 450° to 650 °C can be further cooled to produce lower pressure steam (e.g., steam having a pressure from 3 to 35 bar).
  • the tubes 24 in the transfer line exchanger depicted in Fig. 1 are illustrated as being continuous from the first tube sheet 23 to the second tube sheet 33a. Due to the fact that the two cooling fluids in a transfer-line exchanger of the present invention are of different temperatures, thermal stresses can occur in the tubes if a single tube was to be employed to carry the high temperature fluid over the entire length of the transfer-line exchanger or if the separate tubes of sedtion 10 were mechanically fixed or welded at both ends. In the present invention the transfer-line exchanger is designed such that the thermal stresses do not cause significant problems in cases, e.g., the cooling of a cracked reaction product, where the two cooling fluids have significantly different temperatures. In such cases, it is desirable to compensate for the thermal stresses developed in the tube(s).
  • Fig. 2 depicts that the tubes 24 are npt continuous over the length of both the first and second heat exchanging zones 20 and 30.
  • the tubes are discontinuous with a first portion 24A extending through the first heat exchanging zone 20 and a second portion 24B extending through the second heat exchanging zone 30.
  • a third or intermediate portion 24C of the tube provides fluid communication between tube portions 24A and 24B.
  • the intermediate tube 24C is not physically connected to either tube portions 24A or 24B (i.e., a totally loose connection is provided between tubes 24A, 24B and 24C) and is preferably of the same or substantially the same diameter as the tube portions 24A and 24B. Due to the fact that the tube portions 24A, 24B and 24C are not physically connected, thermal stresses developed during operation of the transfer-line exchanger are reduced. Moreover, this can be achieved without a significant and undesirable pressure drop.
  • Fig. 2 depicts the outlet end of the first heat exchanger zone 20 and the inlet of the second heat exchanger zone 30 of the transfer-line exchanger depicted in Fig. 1.
  • the depicted portion of the first heat exchanger zone comprises tubes 24A which terminate at or near the outlet of the first heat exchanger zone 20.
  • the depicted portion of the second heat exchanger zone 30 comprises tubes 24B which terminate at or near the inlet end of the second heat exchanging zone 30.
  • a tube 24C of the same size and shape as tubes 24A and 24B is placed between the ends of tubes 24A and 24B.
  • the tube 24C is of a length such that it is slightly shorter than the length between the ends of tube 24A and 24B.
  • Guide sleeves or rings 11 and 12 fixed on tube sheets 23a and 33 enclose or encircle a part of the length of each tube 24C at that point where 24C meet the ends of tubes 24A and 24B respectively.
  • the guide sleeve 11 is designed to correctly position the intermediate tube 24C in relation to tubes 24A and 24B.
  • a guide or support baffle (not shown) can also be employed for this purpose.
  • the intermediate tubes are positioned within a tight compartment.
  • the intermediate zone or compartment 10 defined by tube sheets 23a and 33 and flanges 13 and 14 forms a tight compartment having no or essentially no leakage to the environment.
  • Fig. 3 depicts a transfer-line exchanger of the present invention having "double tube" type conduits for the heat exchange operation.
  • the double tube type conduits can be placed in an outer shell, no outer shell encompassing the tube bundle is conventionally employed.
  • the depicted transfer-line exchanger of the double tube type arrangement comprises a first heat exchanging zone 40, a second heat exchanging zone 50 and an intermediate zone 110.
  • An inner conduit 43 for carrying the higher temperature fluid extends through the first heat exchanging zone 40, the intermediate zone 110 and the second heat exchanging zone 50.
  • the conduit 43 is discontinuous with a first portion 43A extending through the first heat exchaning zone 40, a second portion 43B extending through the second heat exchanging zone 50 and an intermediate portion 43C extending between 43A and 43B in the compartment 110.
  • the conduit 43A is enclosed by outer conduits 42 which carry the lower temperature or cooling fluid.
  • outer conduits 52 At opposite ends of conduit 42 are an inlet or distribution pipe or header 41 for receiving the first cooling fluid and an outlet or collection pipe or header 44 for removing the first cooling fluid.
  • outer conduits 52 for carrying the second cooling fluid enclose the second tube portion 43B.
  • the depicted transfer line exchanger also comprises a distribution header 45, connected to an inlet 46, for distributing the high temperature fluid through the inner conduits 43 and a collection header 55, connected to outlet 56 for collecting the cooled, high temperature fluid flowing from the conduits 43.
  • the thermal stresses occurring in the tubes 43 due to the different temperatures of the first and second cooling fluids are reduced in a manner similar to that described hereinbefore.
  • This is illustrated in Fig. 3 and, in more detail, in Fig. 4 which depicts a portion of the outlet end of the first heat exchanging zone 40, the inlet end of the second heat exchanging zone 50 and the intermediate zone 110.
  • the inner conduit 43A is terminated at or near the outlet of the first heat exchanger zone 40.
  • the conduit 43B terminates at or near the inlet end of the second heat exchanging zone 50.
  • a . conduit 43C having the same.
  • conduit .43A and 43B is placed between the end -of conduit 43A and -the end of conduit 438.
  • Guide or ring sleeves 150 and 152 enclose or encircle a small portion of each end portion of conduit 43C at that point where conduits 43A and 43C and 43B and 43C meet.
  • the high temperature fluid is flowed, as indicated by the arrow identified by numeral 80, via the inlet 46 to distribution header 45. From distribution header 45, the high temperature fluid flows into the inner conduits 43 extending through the first heat exchanging zone 40.
  • a first cooling fluid is flowed, as indicated by the arrows identified by numeral 81, from the first distribution pipe 41 through the outer conduits 42 cocurrent with the high temperature fluid flowing through inner conduits 43. As the cooling fluid flows through the outer conduit 42 it cools the high temperature fluid flowing through the inner conduit 43 and is simultaneously heated. The cooling fluid then flows, as indicated by the arrows identified by numeral 82, from the outer conduit 42 into the first collection pipe 44.
  • This cooling fluid which has been heated and/or undergone a phase change in the heat transfer operation then flows from the transfer-line exchanger to a collection point for further use in producing energy or heat.
  • the now partially cooled high temperature fluid flows from the first heat exchanging zone 40 through the intermediate compartment 110 into the second heat exchanging zone 50.
  • a second cooling fluid is flowed from the second distribution pipe 51 through the outer conduits enclosing conduits 43 in the second heat exchanging zone cocurrent with the flow of the partially cooled, high temperature fluid.
  • the cooled high temperature fluid flows, as indicated by the arrow identified by numeral 90, from inner conduit 43 into a collection header 55 and from the transfer line exchanger via outlet 56.
  • the second fluid flows, as indicated by arrows 86, from the outer conduit 52 into collection pipe 54. From the second outlet header, the cooling fluid which has been heated to a higher temperature and/or undergone a phase change, is passed from the transfer-line exchanger for further use in the production of heat and/or energy.
  • the size and shape of the transfer-line exchanger, the first and second heat exchanging zones or compartments, and each element thereof, e.g., the conduits, tube sheets and housings, are selected-on the basis of the end use application and operating conditions of the heat exchanger, including fluctuations in temperature and pressure expected in the operations using the transfer-line exchanger.
  • each of the component parts of the transfer-line exchanger are dependent on a variety of factors including the specific fluids employed and the temperatures and pressures and the materials of construction are selected accordingly. Since the heat exchanger is particularly useful in cooling the cracked reaction product of a hydrocarbop. cracker, the high temperature fluid will have an initial temperature of from 700 to 1100oC or greater. Therefore, the transfer-line exchanger and its component parts must be constructed accordingly. At these temperatures, nickel and nickel-based steel alloys and steel alloys of chromium and molibdinum can be employed in constructing the transfer-line exchanger. In general, steel alloys with molibdinum are sufficient in most applications.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
EP86200931A 1985-05-28 1986-05-28 Refroidisseur de conduit de transfert Withdrawn EP0205205A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL8501514A NL8501514A (nl) 1985-05-28 1985-05-28 Overdrachts-leiding-warmteuitwisselaar.
NL8501514 1985-05-28

Publications (1)

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EP0205205A1 true EP0205205A1 (fr) 1986-12-17

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EP86200931A Withdrawn EP0205205A1 (fr) 1985-05-28 1986-05-28 Refroidisseur de conduit de transfert

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NL (1) NL8501514A (fr)

Cited By (17)

* Cited by examiner, † Cited by third party
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US5591404A (en) * 1991-09-25 1997-01-07 Mathewson; Wilfred Integrated low priming volume centrifugal pump and membrane oxygenator
EP1198996A3 (fr) * 2000-08-09 2003-09-24 Sasib S.p.A. Appareil de chauffage et de contrôle de température pour tunnel de pasteurisation
NL1021111C2 (nl) * 2002-07-19 2004-01-23 Bloksma B V Koelinrichting.
WO2004083758A3 (fr) * 2003-03-21 2005-04-14 Behr Gmbh & Co Kg Echangeur de la chaleur de gaz de combustion et dispositif d'etancheite de cet echangeur
WO2007008424A1 (fr) * 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Procédé de traitement d’un effluent de la pyrolyse d’hydrocarbures
WO2007008397A1 (fr) 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Procédé de traitement d’un effluent de la pyrolyse d’hydrocarbures
WO2007008406A1 (fr) 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Procede de traitement d'un effluent issu de la pyrolyse d'hydrocarbone
US7674366B2 (en) 2005-07-08 2010-03-09 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7718049B2 (en) 2005-07-08 2010-05-18 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7749372B2 (en) 2005-07-08 2010-07-06 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
WO2012015494A2 (fr) 2010-07-30 2012-02-02 Exxonmobil Chemical Patents Inc. Procédé de traitement d'effluent de pyrolyse d'hydrocarbures
US20130001132A1 (en) * 2010-01-26 2013-01-03 Arthur James Baumgartner Method and apparatus for quenching a hot gaseous stream
US8524070B2 (en) 2005-07-08 2013-09-03 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
WO2015128034A1 (fr) * 2014-02-25 2015-09-03 Saudi Basic Industries Corporation Procédé pour le chauffage de pétrole brut
CN105135917A (zh) * 2015-10-15 2015-12-09 上海锅炉厂有限公司 一种壳程自冷却保护浮头式换热器
CN109696078A (zh) * 2018-12-25 2019-04-30 陕西延长石油（集团）有限责任公司 一种合成气冷却器温度控制系统及其控制方法
CN112298516A (zh) * 2020-11-23 2021-02-02 中国船舶重工集团公司第七0四研究所 串联式多介质单流程式集中冷却中心

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EP1198996A3 (fr) * 2000-08-09 2003-09-24 Sasib S.p.A. Appareil de chauffage et de contrôle de température pour tunnel de pasteurisation
NL1021111C2 (nl) * 2002-07-19 2004-01-23 Bloksma B V Koelinrichting.
EP1382927A3 (fr) * 2002-07-19 2005-09-14 Bloksma B.V. Dispositif de refroidissement
CN100436798C (zh) * 2003-03-21 2008-11-26 贝洱两合公司 废气热交换器
WO2004083758A3 (fr) * 2003-03-21 2005-04-14 Behr Gmbh & Co Kg Echangeur de la chaleur de gaz de combustion et dispositif d'etancheite de cet echangeur
US10358958B2 (en) 2003-03-21 2019-07-23 Mahle International Gmbh Exhaust gas heat exchanger and sealing device for the same
US9279395B2 (en) 2003-03-21 2016-03-08 Mahle International Gmbh Exhaust gas heat exchanger and sealing device for the same
CN101218322B (zh) * 2005-07-08 2011-06-22 埃克森美孚化学专利公司 烃热解排出物的加工方法
EP2330175A2 (fr) 2005-07-08 2011-06-08 ExxonMobil Chemical Patents Inc. Appareil de traitement d'un effluent issu de la pyrolyse d'hydrocarbone
JP2009500493A (ja) * 2005-07-08 2009-01-08 エクソンモービル・ケミカル・パテンツ・インク 炭化水素パイロリシス排出物の処理法
JP2009500492A (ja) * 2005-07-08 2009-01-08 エクソンモービル・ケミカル・パテンツ・インク 炭化水素パイロリシス排出物の処理法
US7674366B2 (en) 2005-07-08 2010-03-09 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7718049B2 (en) 2005-07-08 2010-05-18 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
KR100966962B1 (ko) * 2005-07-08 2010-06-30 엑손모빌 케미칼 패턴츠 인코포레이티드 탄화수소 열분해 유출물을 처리하는 방법
KR100966961B1 (ko) * 2005-07-08 2010-06-30 엑손모빌 케미칼 패턴츠 인코포레이티드 탄화수소 열분해 유출물을 처리하는 방법
US7749372B2 (en) 2005-07-08 2010-07-06 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7763162B2 (en) 2005-07-08 2010-07-27 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7780843B2 (en) 2005-07-08 2010-08-24 ExxonMobil Chemical Company Patents Inc. Method for processing hydrocarbon pyrolysis effluent
WO2007008397A1 (fr) 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Procédé de traitement d’un effluent de la pyrolyse d’hydrocarbures
WO2007008406A1 (fr) 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Procede de traitement d'un effluent issu de la pyrolyse d'hydrocarbone
US7972482B2 (en) 2005-07-08 2011-07-05 Exxonmobile Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7981374B2 (en) 2005-07-08 2011-07-19 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
EP2330175A3 (fr) * 2005-07-08 2011-09-28 ExxonMobil Chemical Patents Inc. Appareil de traitement d'un effluent issu de la pyrolyse d'hydrocarbone
US8074707B2 (en) 2005-07-08 2011-12-13 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US7465388B2 (en) 2005-07-08 2008-12-16 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
CN101218320B (zh) * 2005-07-08 2012-07-04 埃克森美孚化学专利公司 烃热解排出物的加工方法
WO2007008424A1 (fr) * 2005-07-08 2007-01-18 Exxonmobil Chemical Patents Inc. Procédé de traitement d’un effluent de la pyrolyse d’hydrocarbures
US8524070B2 (en) 2005-07-08 2013-09-03 Exxonmobil Chemical Patents Inc. Method for processing hydrocarbon pyrolysis effluent
US20130001132A1 (en) * 2010-01-26 2013-01-03 Arthur James Baumgartner Method and apparatus for quenching a hot gaseous stream
US9175229B2 (en) * 2010-01-26 2015-11-03 Shell Oil Company Method and apparatus for quenching a hot gaseous stream
WO2012015494A2 (fr) 2010-07-30 2012-02-02 Exxonmobil Chemical Patents Inc. Procédé de traitement d'effluent de pyrolyse d'hydrocarbures
CN106062139A (zh) * 2014-02-25 2016-10-26 沙特基础工业公司 用于加热原油的方法
KR20160146678A (ko) * 2014-02-25 2016-12-21 사우디 베이식 인더스트리즈 코포레이션 원유를 가열하는 방법
JP2017512233A (ja) * 2014-02-25 2017-05-18 サウジ ベーシック インダストリーズ コーポレイションＳａｕｄｉ Ｂａｓｉｃ Ｉｎｄｕｓｔｒｉｅｓ Ｃｏｒｐｏｒａｉｔｏｎ 原油の加熱方法
US10000708B2 (en) 2014-02-25 2018-06-19 Saudi Basic Industries Corporation Method for heating crude
WO2015128034A1 (fr) * 2014-02-25 2015-09-03 Saudi Basic Industries Corporation Procédé pour le chauffage de pétrole brut
CN106062139B (zh) * 2014-02-25 2019-09-06 沙特基础工业公司 用于加热原油的方法
CN105135917A (zh) * 2015-10-15 2015-12-09 上海锅炉厂有限公司 一种壳程自冷却保护浮头式换热器
CN109696078A (zh) * 2018-12-25 2019-04-30 陕西延长石油（集团）有限责任公司 一种合成气冷却器温度控制系统及其控制方法
CN112298516A (zh) * 2020-11-23 2021-02-02 中国船舶重工集团公司第七0四研究所 串联式多介质单流程式集中冷却中心

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