US20030070962A1 - Pyrolysis furnace with new type radiant tubes arrangement and method of its operation and usage - Google Patents

Pyrolysis furnace with new type radiant tubes arrangement and method of its operation and usage Download PDF

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Publication number
US20030070962A1
US20030070962A1 US10/246,625 US24662502A US2003070962A1 US 20030070962 A1 US20030070962 A1 US 20030070962A1 US 24662502 A US24662502 A US 24662502A US 2003070962 A1 US2003070962 A1 US 2003070962A1
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US
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Prior art keywords
tubes
radiant
section
pyrolysis furnace
pass
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Abandoned
Application number
US10/246,625
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English (en)
Inventor
Qingquan Zeng
Guoqing Wang
Shixing Xu
Zhaobin Zhang
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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Assigned to CHINA PETROLEUM & CHEMICAL CORPORATION, BEIJING RESEARCH INSTITUTE OF CHEMICAL INDUSTRY reassignment CHINA PETROLEUM & CHEMICAL CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WANG, GUOQING, XU, SHIXING, ZENG, QINGQUAN, ZHANG, ZHAOBIN
Publication of US20030070962A1 publication Critical patent/US20030070962A1/en
Abandoned legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/2425—Tubular reactors in parallel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00085—Plates; Jackets; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00157—Controlling the temperature by means of a burner

Definitions

  • the invention relates to a pyrolysis furnace and method of its operation and usage, specially relates to a pyrolysis furnace with new type radiant tubes arrangement for high temperature cracking reaction of Hydrocarbons, and the method of its operation and usage.
  • the radiant tubes employing single row arrangement in radiant section receive double-wall radiation; they have the most uniform heat receiving and best heat conducting effect. But the disadvantage is that in same area the number of tubes capable to be arranged is minimum, the productivity of specific area is low. Under this condition of single row arrangement, in order to meet the requirement of magnification of pyrolysis furnace, it needs to extend the length of every radiant tubes or the length of radiant section, an inexorable result is that we have to greatly increase the height and length of radiant section and meet the more severe requirement for uniform heat supply by burners in radiant section. At same time extremely long radiant tube makes the engineering problems complicated. Therefore, the use of single row arrangement structure significantly limits the productivity of pyrolysis furnace.
  • FIG. 6 shows an arrangement of prior art of two pass branched radiant tubes 7 with different diameters of type 2 - 1 in radiant section 3 , wherein the first pass and second pass tubes are located in a same plane, this is a single row arrangement. It can be seen that although the tubes uniformly receive heat, but not so many tubes are arranged in radiant section, the space utilization is not high, as well as the arrangement of tubes is not symmetrical and tube lengths are not the same, this leads to different working condition of cracking process in various tubes, and thus the cracking effect is affected.
  • high temperature condition of cracking reaction is achieved by heat supply from burners to radiant tubes in the radiant section.
  • the burners are divided into bottom burners, wall burners and top burners.
  • Abovementioned pyrolysis furnace of prior art generally comprising: a convection section, used for preheating the hydrocarbons feed stock; a radiant section, used for high temperature cracking hydrocarbons feedstock; and crossover section, connected between the convection section and radiant section.
  • a typical pyrolysis furnace with bottom burning manner is shown in FIG. 5, wherein bottom burners 8 and multiple groups of radiant tubes 7 are arranged in radiant section 3 ; the convection section is located above the radiant section and axially shifted therewith, wherein multiple groups of convection tubes 1 are arranged; a crossover section 6 is passed horizontally from top portion of radiant section to connect with bottom portion of convection section.
  • the above mentioned pyrolysis furnace of prior art has greater overall height, it increases design and technology difficulty and results in larger amount of capital expenditure at same time.
  • the object of the present invention is to provide a pyrolysis furnace with new type radiant tubes arrangement in radiant section, which has the feature of simple employ, excellent heat conduction, small investment, easy maintenance, and flexible control.
  • said multiple groups radiant tubes are two pass tubes with different diameters, the first pass tubes and second pass tubes are located at two parallel planes, more over, the projection of each second pass tube is corresponding to the center line of projection connecting line of two first pass tubes, adjacent therewith, the structure of each first pass and second pass tube is the same.
  • said radiant tubes may be two pass non-branched tubes with different diameters (type 1 - 1 ) or two pass branched tubes with different diameters (type 2 - 1 , 4 - 1 ), wherein the two pass branched tubes with different diameters (type 2 - 1 ) are particularly preferred.
  • the pitch between two adjacent radiant tubes in said same plane is 1.8 ⁇ 6.0 times of outer diameter of the radiant tubes, preferably, 1.8 ⁇ 4.2 times, more preferably, 2.0 ⁇ 2.8 times
  • the distance between the planes where said first pass tubes and second pass tubes are located is 100 ⁇ 600 mm, preferably, 200 ⁇ 500 mm, most preferably, 300 ⁇ 400 mm.
  • the pyrolysis furnace of this invention may also employ a new type heat supply manner, wherein top burners and bottom burners are simultaneously arranged in said radiant section, and said crossover section is extended from middle-upper portion of radiant section wall, and connected to bottom portion of convection section.
  • FIG. 1 is a diagrammatic elevation view of a new type pyrolysis furnace according to the present invention.
  • FIG. 2 is a top view of radiant section of pyrolysis furnace according to the present invention, taking as an example, the radiant tubes are type 2 - 1 ;
  • FIG. 3 is an elevation view of FIG. 2 wherein two groups of radiant tubes are shown;
  • FIG. 4 is a side view of FIG. 2;
  • FIG. 5 is a diagrammatic view of a typical pyrolysis furnace employing bottom burners heat supply in the prior art
  • FIG. 6 is a diagrammatic top view and elevation view of a single row arrangement of radiant tubes in a pyrolysis furnace in the prior art.
  • the new type pyrolysis furnace of this invention comprising radiant section 3 ; bottom burners 8 , arranged in radiant section 3 ; multiple groups of two pass non-branched tubes with different diameters 7 (type 1 - 1 ) or two pass branched tubes with different diameters 7 (type 2 - 1 , 4 - 1 ), vertically arranged in radiant section; wherein, tubes with different diameters means that the first pass tube and second pass tube in two pass tubes has different diameter, but two or four first pass tubes in two pass tubes type 2 - 1 , 4 - 1 should have same diameter; convection section 2 , shifted from radiant section 3 ; multiple groups of convection tubes 1 , horizontally arranged in convection section 2 ; crossover section 6 , horizontally arranged between radian section 3 and convection section 2 ;
  • the feedstock for cracking is introduced from the convection tubes 1 in convection section of furnace through the crossover tube 5 of convection tubes 1 into radiant tubes 7 , then successively pass through the first pass tubes (1 tube, 2 tubes or 4 tubes) of radiant tubes 7 , second pass tube (1 tube), at last pass from outlet of second pass tube of radiant tubes 7 into Transfer Line Exchange(TLE) 4 .
  • said radiant tubes may be two pass non-branched tubes with different diameters (type 1 - 1 ) or two pass branched tubes with different diameters (type 2 - 1 ), wherein the two pass branched tubes with different diameters (type 2 - 1 ) are particularly preferred.
  • the first pass tubes and second pass tubes of various groups are located at two parallel planes respectively, and the projection of each second pass tubes is corresponding to the center location of projection connecting line of two first pass tubes, adjacent there with, and the structure of each first tube and second tube is the same respectively, wherein the pitch between two adjacent radiant tubes in said same plane is 1.8 ⁇ 6.0 times of outer diameter of the radiant tubes, preferably, 1.8 ⁇ 4.2 times, more preferably, 2.0 ⁇ 2.8 times; the distance between first pass tubes and second pass tubes of each group is 100 ⁇ 600 mm, preferably, 200 ⁇ 500 mm, most preferably, 300 ⁇ 400 mm.
  • the present invention employs new type arrangement of radiant tubes, so as to make the pitch between two adjacent radiant tubes in same plane to be just right, the bends of radiant tubes of radiant section in various groups and manifold are parallel each other without cross link, this has no influence on radiant heat conduction of radiant tubes in various groups, simultaneously, the form and weight of bends of radiant tubes in various groups and manifold are fully the same, these components have high versatility, and are simple for manufacture and maintenance; the overall length of radiant tubes of radiant section in various groups are fully the same, the residence time and pressure drop of feedstock are fully the same, which is easy to optimization of employ and control; the weight of radiant tubes of radiant section in various groups is fully the same, this makes the balance and suspension system easy to be arranged and regulated.
  • top burners 9 can also be added in radiant section, as shown in FIG. 1.
  • the location of the crossover section 6 can be determined by the top/bottom burners' heat supply ratio R of different pyrolysis furnaces.
  • the top wall of crossover section is located under the top wall of radiant section, its distance H is 10% ⁇ 50% of total height of radiant section wall, preferably, R varies in a range of 2:8 ⁇ 6:4, H is 10% ⁇ 40% of total height of radiant section wall; more preferably, R varies in a range of 2.5: 7.5 ⁇ 5:5, H is 15% ⁇ 40% of total height of radiant section wall, most preferably, R varies in a range of 3:7 ⁇ 4:6, H is 20% ⁇ 40% of total height of radiant section wall.
  • top burners and bottom burners can be used to supply all heat need for high temperature cracking top burners and bottom burners may be, preferably combined oil-gas burners.
  • said pyrolysis furnace can employ top burners and bottom burners of same amount.
  • the top or bottom burners may be arranged symmetrically about centerline of top or bottom portion, the ratio of numbers of top/bottom burners is equal to, and corresponding to one another at top and bottom portions, moreover, the top/bottom burners heat supply ratio R can be controlled by controlling the top/bottom burners fuel feeding ratio.
  • a pyrolysis furnace according to a preferred embodiment of this invention, wherein the used top burners and bottom burners may be burners of various kinds, as known to a person skilled in the art. In order to reduce cost, preferably employ conventional burners.
  • the present invention can reduce the number of burners, so as to reduce the investment and simplify the structure of pyrolysis furnace; moreover, the present invention can fully are the conventional burners, as top and bottom burners, which can be produced in our country, and is inexpensive, and simple in employ and maintenance.
  • top and bottom burners combined heat supply manner due to employ of top and bottom burners combined heat supply manner, the temperature distribution is relatively uniform, at the same time the top/bottom burners heat supply ratio R can be adjusted in period of design according to the structure requirements, thus the design flexibility is greatly increased; in addition, employ of top and bottom burners combined heat supply manner of this invention, the outlet of fuel gas of cross over section, which is located at top portion of radiant section of traditional art, is shifted down to middle-upper portion of radiant section, this not bring about negative influence on the cracking effect of pyrolysis furnace, but makes the height of convection section 2 to shift down, so that the overall height of pyrolysis furnace may be lowered (by 3 ⁇ 6 m in average, the particular height is controlled by top/bottom burners heat supply ratio R).
  • a pyrolysis furnace has the yield of ethylene of 100 kiloton per year.
  • Said pyrolysis furnace comprising: a radiant section with furnace chamber height of about 17 m; a convection section shifted from radiant section, with height about 15 m; a cross over section, horizontally arranged and extended between said radiant and convection sections, the upper edge of outlet of crossover section is located about 6 m below from the top portion of furnace chamber; 24 top burners, arranged symmetrically about the center line of top portion, and 24 bottom burners arranged symmetrically about the center line of bottom portion; multiple groups of convection tubes, horizontally arranged in convection section, and 48 groups of radiant tubes (type 2 - 1 ), vertically arranged in radiant section.
  • crossover section Because the location of crossover section is shifted down about 6 m, the over all height of furnace is cut down about 6 m, where as the former pyrolysis furnace of the same scale, employing wall and bottom burners combined heat supply manner need to comprise 24 bottom burners and 48 wall burners.
  • the furnace employ former staggered row arrangement of radiant tubes, by only possibility is to arrange 48 groups of radiant tubes (type 2 - 1 ), the bends of adjacent groups and manifolds are located in different heights, as well as in different planes, the distance between is 1.8 times of outer diameter of radiant tubes, the length of of furnace chamber is about 20 m.
  • the radiant tubes are arranged by the arrangement manner of the present invention, all the first pass tubes are located at one plane, all the second pass tubes are located at another plane, the distance between two planes is 320 mm, when the distance between first pass tubes is 2.4 times of outer diameter thereof, and the distance between second pass tubes is 3.5 times of outer diameter thereof, 64 groups of radiant tubes (type 2 - 1 ) can be arranged in the same furnace chamber, this increases the productivity by 33%;
  • the radiant tubes are arranged by the arrangement manner of the present invention, when the distance between first pass tubes is 2.8 times of outer diameter thereof, and the distance between second pass tubes is 4.1 times of outer diameter thereof, 54 groups of radiant tubes (type 2 - 1 ) can be arranged in the same furnace chamber, this increases the productivity by 12.5%, at this time due to the distance between adjacent radiant tubes is increased, more uniform radiant conduction is obtained, this case is apparently advantageous for revamping old furnaces, and can remarkably increase productivity under condition of minimum investment.
  • the hydrocarbons feedstock and dilution steam mixture passes through multi-path convection tubes 1 , horizontally extended in convection section 2 , after recovering the heat of fuel gas in convection section and preheating to the temperature of crossover section, the hydro carbons feedstock passes through the convection tubes 1 into cross tube 5 , after distributing an appropriate current by distributor, into radiant tubes 7 , vertically arranged in radiant section 3 , the cracked product is heat exchanged in transfer line exchanger 4 .
  • the pyrolysis furnace is fully based on the heat supplied by bottom burners 8 and top burners 9 , and at same time the fuel gas, produced from top and bottom burners passes through the horizontally arranged crossover section 6 , providing convection heat to convection section 2 .
  • a pyrolysis furnace has the yield of ethylene of 60 kilo-ton per year, said pyrolysis furnace comprising: a radiant section with furnace chamber height of about 14 m; a convection section, shifted from radiant section, with height about 14 m; a crossover section, horizontally arranged and extended between said radiant section and convection section; the upper edge of outlet of cross over section is located about 3 m from top portion of furnace chamber; 24 top burners arranged symmetrically about the center line of top portion, and 24 bottom burners, arranged symmetrically about the center line of bottom portion; multiple groups of convection tubes, horizontally arranged in convection section, and 32 groups of radiant tubes (type 2 - 1 ), vertically arranged in radiant section.
  • the radiant tubes are arranged by former single row arrangement, the length of furnace chamber is about 15 m, the radiant tubes are two pass non-branched tubes (type 1 - 1 ), In order to avoid the mutual overlap radiant tubes bends and connected tubes in lower portion of furnace chamber, the distance between first pass tubes is 2.8 times of outer diameter thereof, and the distance between second pass tubes is 2.3 times of outer diameter thereof, in addition, it is a single row arrangement, only 48 groups radiant tubes can be arranged.
  • the radiant tubes employ the arrangement manner of the present invention, all the first pass tubes are located at one plane, and all the second pass tubes are located at another plane, the distance between two planes is 350 mm, when the distance between first pass tubes is 2.8 times of outer diameter thereof, and the distance between second pass tubes is 2.3 times of outer diameter thereof, the radiant tubes employ the arrangement manner of the present invention, 108 groups two pass non-branched tubes with different diameters (type 1 - 1 ) can be arranged, this increases productivity to about 220%, at same time, various radiant tubes have uniform heat conduction, in addition, the form and weight of bends in various groups and manifold are fully the same, these components have high versatility, and all bends and connected tubes are parallel arranged in lower portion of furnace chamber, without interference, and are simple for manufacture and maintenance.
  • the pyrolysis furnace is fully based on the heat, supplied by bottom burners 8 and top burners 9 , and at the same time, the fuel gas, produced from top and bottom burners passes through the horizontally arranged crossover section 6 , providing convection heat to the convection section 2 .
  • a pyrolysis furnace has the same pyrolysis furnace of example 1, but employing radiant tubes type 4 - 1 .
  • the distance between first pass tubes is about 1.8 times of the outer diameter thereof
  • the distance between second pass tubes is about 1.4 times of the outer diameter thereof
  • 32 groups of radiant tubes can be arranged, instead, employing the arrangement manner of radiant tubes of the present invention, the distance between first pass tubes still maintain 1.8 times of the outer diameter thereof, but the distance between second pass tubes is increased to 3.8 times of the outer diameter there of, all the first pass tubes are located at one plane, all the second pass tubes are located at another plane, the distance between two planes is 350 mm, This increases the productivity by about 50%.
  • first pass tubes enlarged to 2.4 times of the outer diameter thereof, the distance between second pass tubes enlarged to 5.1 times of outer diameter there of, and the distance between first and second pass tubes is 350 mm, in this case, 36 groups of radiant tubes can be arranged, this increases the productivity by about 12%, at this time, due to the enlargement of distance between tubes, the ability for radiant convection by radiant tubes is far better than radiant tubes-employing single row arrangement.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US10/246,625 2001-09-19 2002-09-19 Pyrolysis furnace with new type radiant tubes arrangement and method of its operation and usage Abandoned US20030070962A1 (en)

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CNB011417722A CN1194071C (zh) 2001-09-19 2001-09-19 裂解炉及其用途
CN01141772.2 2001-09-19

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090022635A1 (en) * 2007-07-20 2009-01-22 Selas Fluid Processing Corporation High-performance cracker
US20120020852A1 (en) * 2008-10-16 2012-01-26 Xiou He ethylene cracking furnace

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9205400B2 (en) 2011-07-28 2015-12-08 China Petroleum & Chemical Corporation Ethylene cracking furnace
CA2879945C (en) 2012-08-07 2019-12-31 Foster Wheeler Usa Corporation Method and system for improving spatial efficiency of a furnace system
CN104449803B (zh) * 2013-09-13 2016-08-17 中国石油化工股份有限公司 一种烯烃的生产方法
CN111712558B (zh) * 2017-12-29 2022-06-14 埃克森美孚化学专利公司 烃热解中的焦炭减轻

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US2112224A (en) * 1932-02-15 1938-03-29 Universal Oil Prod Co Radiant heat furnace
US2415726A (en) * 1943-12-02 1947-02-11 Phillips Petroleum Co Apparatus for heating oils
US3841274A (en) * 1973-11-29 1974-10-15 Universal Oil Prod Co High temperature heater for fluids
US4342642A (en) * 1978-05-30 1982-08-03 The Lummus Company Steam pyrolysis of hydrocarbons
US4361478A (en) * 1978-12-14 1982-11-30 Linde Aktiengesellschaft Method of preheating hydrocarbons for thermal cracking
US5181990A (en) * 1986-01-16 1993-01-26 Babcock-Hitachi Kabushiki Kaisha Pyrolysis furnace for olefin production
US4879020A (en) * 1987-05-08 1989-11-07 Kinetics Technology International Method of operating a furnace hydrocarbon converter
US4999089A (en) * 1988-09-30 1991-03-12 Mitsui Engineering & Shipbuilidng Co., Ltd. Cracking furnace
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090022635A1 (en) * 2007-07-20 2009-01-22 Selas Fluid Processing Corporation High-performance cracker
US20120020852A1 (en) * 2008-10-16 2012-01-26 Xiou He ethylene cracking furnace
US8916030B2 (en) * 2008-10-16 2014-12-23 China Petroleum & Chemical Corp. Ethylene cracking furnace

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CN1194071C (zh) 2005-03-23
CN1405273A (zh) 2003-03-26
EP1295930B1 (en) 2011-07-27
EP1295930A1 (en) 2003-03-26

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Effective date: 20021021

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION