US3227525A - Apparatus for pyrolyzing vapors - Google Patents

Apparatus for pyrolyzing vapors Download PDF

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Publication number
US3227525A
US3227525A US388346A US38834664A US3227525A US 3227525 A US3227525 A US 3227525A US 388346 A US388346 A US 388346A US 38834664 A US38834664 A US 38834664A US 3227525 A US3227525 A US 3227525A
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tube
benzene
diphenyl
pipe
vapor
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Expired - Lifetime
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US388346A
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English (en)
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Marcel E Degeorges
Jaymond Maurice
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Progil SARL
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Progil SARL
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
    • C10G9/18—Apparatus
    • C10G9/20—Tube furnaces
    • 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
    • B01J19/2405—Stationary reactors without moving elements inside provoking a turbulent flow of the reactants, such as in cyclones, or having a high Reynolds-number
    • 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
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/008—Pyrolysis reactions
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
    • 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
    • B01J2219/00101—Reflux columns
    • 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
    • B01J2219/00132—Controlling the temperature using electric heating or cooling elements
    • 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
    • B01J2219/0015—Controlling the temperature by thermal insulation means
    • B01J2219/00155—Controlling the temperature by thermal insulation means using insulating materials or refractories

Definitions

  • This invention relates to apparatus for pyrolyzing vapors and, more particularly, to apparatus arranged to cause a chemical reaction in chemical vapors by passing the vapors through a tube to the exterior of which heat is applied.
  • pyrolyzation apparatus in the past have been capable of only very inefiicient operation. For instance, in the pyrolysis of benzene vapors to obtain diphenyl, only 5% of the benzene vapors in a given pass through the tubing have been converted; furthermore, the conversion has taken place in such a manner that only approximately 90% of the conversion was to diphenyl, the remainder being undesired elements, such as polyphenyls, tar, and carbon.
  • the biggest problem in pyrolyzation apparatus in the past has been the accumulation of carbon and tar on the inside surface of the tubes so that the process could be carried on for only a short time before it was necessary to shut down the apparatus and clean the tubes.
  • Another object of this invention is the provision of a pyrolysis apparatus making use of tubes of relatively large diameter whereby the heat exchange portions are very simple and free of maintenance.
  • a further object of the present invention is the provision of a high production pyrolysis apparatus which is relatively free of the problem of coating of the inside surfaces of the tube by carbon or tars.
  • a still further object of this invention is the provision of pyrolyzation apparatus for hydrocarbon vapors making use of a small number of relatively large diameter tubes and operating with vapor flow of extremely high turbulence whereby extremely high conversion rates take place.
  • FIG. 1 is a somewhat schematic view of apparatus embodying the principles of the present invention.
  • FIG. 2 is an isometric view with portions broken away of a portion of the apparatus.
  • FIG. 1 which best shows the general features of an apparatus embodying the principles of the invention
  • a pyrolysis apparatus indicated generally by the reference numeral 10
  • the vaporizer is provided with a heating coil 17 connected to a source of heating steam (not shown). It is also provided with another coil 18 whose use will be described further hereinafter.
  • a pipe 19 connects the pipe 15 of the vaporizer 16 to a tubular heat exchanger 21, the other end of which is connected to a pyrolysis furnace 23 having a tube 24 which will be described in greater detail later.
  • the entrance end of the tube 24 is connected to the pipe 22 and the other end is connected through a pipe 25 to a tube 26 lying within the heat exchanger 21.
  • the other end of the tube 26 is connected by a pipe 27 to one end of the coil 18 which lies in the vaporizer 16.
  • the other end of the coil 18 is connected by a pipe 28 to the lower end of a fractionating column 29.
  • the central portion of the fractionating column 14 is connected to a reflux regulator valve 31.
  • the upper part of the fractionating column 29 is connected to the upper part of a condenser 32, the bottom of which is connected to a cylinder- 33, the bottom ofwhich is connected by a pipe 34 to the storage tank 12.
  • the top of the cylinder 33 is connected to a cooler 35 having a top eXit pipe 36 from which hydrogen or other generated gas can be removed.
  • the bottom of the fractionating column 29 'passes into the top of a second column 37 having a heating coil 38.
  • any benzene remaining is distilled off through a pipe 39 lead. ing back to the first column 29.
  • the bottom of the colrnun 37 is connected by a pipe 41 to a third colmun 42 having a heating coil 43 at its lower portion.
  • a reflux coil 44 is located at the upper part of the column 42 and is connected through a valve 45 to a water storage container 46.
  • the water which may be evaporated in the coil 44 passes through a pipe 47 to a condenser 48, the bottom of which is connected by a pipe 49 to the top of the water storage tank 46.
  • the top of the column 42 is connected by a pipe 51 to a coil 52 lying in a vessel 53.
  • the coil 52 is completely immersed in a body 54 of boiling water the vapor from which is condensed by a cooling coil 55 located in the upper part of the vessel 53. Finally, pure product, such as diphenyl, leaving the bottom of the coil 52 through a pipe 56 which is connected to a storage drum 57. Similarly, the bottom of the column 42 is connected by a pipe 58 to a drum 59 in which the undesired higher molecular weight products, such as polyphenyls are stored.
  • the pyrolysis furnace 23 is shown in detail in FIG. 2.
  • the furnace is provided with a vertical tubular steel wall 61 which is lined with insulating material 62 in which are embedded electrical heating elements 63. Lying within the housing defined by the wall 61 and the insulating material 62 is the coil 24 which is arranged in a series of convolutions lying in an imaginary cylinder coaxial with the wall 61.
  • the entrance pipe 22 is connected to the coil as is the exit pipe 25.
  • Each convolution consists of a U-shaped bend 64 which merge into vertical straight portions 65.
  • the inside diameter of the tube 24 may be selected in the range between 55 and 205 mm.
  • One of the factors which must be taken into account in selecting the diameter is the desired hourly production of the product, such as diphenyl.
  • suitable diversification of production may be obtained with a pyrolysis tube having a diameter in the range between 80 mm. and 140 mm. with best results in the range of from 100 to 120 mm.
  • the length of the tube is, of course, determined by the exact process and the diameter of the tube.
  • the tubes should be made of refractory steel.
  • the tube is bent in a plurality of portions of its length; however, it is advisable that the tube have a bend every length in the range of from 2 to meters with preference being given to the range of from 3 to 5 meters.
  • the bends of the tube 24 have their radius of curvature as little as possible compatible with the diameter of the tube. It is preferable that the radius of the axis of the tube in the bend be of the same order as the external diameter of the tube; good results are obtained when the radii equal 1 or 2 times the outside diameter.
  • the straight parts 65 form an angle to one another as close as possible to 0, and in any case, an angle of less than 30. With the radius of curvature selected in the manner shown, the distance between two successive straight portions 65 will be in the same order as the outside diameter of the tube.
  • Benzene vapor then passes through the pipe 22 into the pyrolysis furnace 23. After passing through the coil 24 in which the reaction takes place, the pyrolyzed vapors when leaving the furnace by the pipe 25 now contain benzene, diphenyl, polyphenyls, and hydrogen. These then pass through the heat exchange tube 26 in the heat exchanger 21 and then through the pipe 27 into the coil 18 within the vaporizer 16. There heat passes into the fresh benzene in the tube 15 as it comes from the storage tank 12. These vapors are conducted by the pipe 28 to the bottom of the first column 29 in which the benzene is separated from the pyrolysate. Benzene distilled in the column 29 is liquified by the condenser 32.
  • the central region of the column 29 is kept at constant temperature by means of the reflux regulator valve 31. From the condenser 32 liquid benzene flows into the intermediate cylinder 33 from which it returns to the storage tank 12. So far as the hydrogen evolved is concerned, it is cooled to a low temperature within the cooler 35 in order to recover any benzene it carries before it is taken away at the top through the pipe 36.
  • Crude diphenyl (which still contains polyphenyls and also a little benzene) is the liquid fraction recovered at the bottom of the column 29, and this is permitted to run into the second column 37 having the heating coil 38 in its lower portion. From the column 37 the remainder of the benzene distills off to the column 29, while a mixture of diphenyl and polyphenyls enter the third distillation column 42. These two elements are then separated. The heat required for the separation is provided by the heating coil 42 at the bottom of the column. Adequate reflux is obtained at the top of the column 42 by circulating water through the coil 44, the inlet of which is provided with the valve 45.
  • Water vaporized within the coil 44 liquifies in the condenser 48 from which it returns through the pipe 49 to the storage container 46, the lower part of which is connected with the coil 44 through the valve 24.
  • Purified diphenyl vapor which leaves the top of the column 42, is condensed to the liquid state within the coil 52 in the vessel 53.
  • This coil is situated in the bottom part of the vessel 53 and the vessel contains the body 54 of boiling water suflicient for the coil 52 to be completely immersed. As the water boils, its vapor is condensed in the upper coil 55 within which cold water is circulated. In this way, the condensation of pure diphenyl is formed without any crystallization of this compound within the coil 52.
  • Example I In an installation similar to that shown in FIG. 1, 3,000 kilograms of diphenyl were produced continuously each 24 hour period.
  • the furnace in reaction tube was similar to those shown in FIG. 2.
  • the tube was 50 meters long and had 11 successive bends, so that there were 12 straight portions of about 4.08 meters each.
  • the internal diameter of the tube was mm. and the radius of curvature of the bends at the axis of the tube was mm.
  • the distance between the axes of two adjacent straight portions was about 235 mm.
  • the temperature of the henzene vapor entering the apparatus through the pipe 22 was 560 C. and the heating by means of coil 63 was so controlled that the vapor left the apparatus through the pipe 25 at a temperature of 800 C.
  • the tube was continuously fed with 1390 kilograms per hour of benzene vapor.
  • the flowing vapor remained within the tube 24 for 1.32 seconds, which means that the vapor flowed with a linear velocity of 38.4 meters per second.
  • the average Reynolds number of the vapor therefore, was 180,000.
  • With each passage of the vapor through the pyrolysis tube 9% of the benzene was converted into diphenyl with a yield of 92%. There was practically no formation of tar or carbon within the reaction tube and the tube worked formation.
  • the pyrolysis tube In a process carried on in the manner similar to that :of Example I, the pyrolysis tube, however, was 67 meters long, instead of 50 meters.
  • the benzene vapor entered through the pipe 22 at 600 C. and left the tube 24 through the pipe 25 at a temperature of 750 C.
  • the time of its passage through the pyrolysis zone was 1 second and the Reynolds number was 320,000.
  • 10% of the benzene was transformed into diphenyl with a yield of 87%.
  • 4.5 tons of diphenyl was thus produced every 24 hours and it was possible to vary the daily production between 1.5 and 5 tons with the same reaction tube.
  • the above results should be compared with tests carried out according to the prior art at the same average temperature of 675 C.
  • Example 111 A production of 6 tons of diphenyl per 24 hours was carried'on with a single pyrolysis tube 67 meters long in an apparatus otherwise similar to that used in Example II.
  • Example IV With the apparatus used in Example I equipped, however, with a reaction tube having an internal diameter of Benzene vapor remained within the tube was for 0.3 second at a mean temperature of 765 C. (inlet temperature 700 C. and outlet temperature 830 C.) and its turbulence corresponded to a Reynolds number of 460,000. Under these conditions 3.3 tons of diphenyl were prepared every 24 hours with a conversion rate of benzene of 3.5% at each passage and a yield of 96.6%.
  • Example VI The production of diphenyl was effected within a pyrolysis tube 96 meters long having an internal diameter of 200 mm.
  • the benzene vapor entered the tube at 406 C. and left it at 710 C., the mean temperature being 585 C.
  • the vapor passed through the tube in 2.7 secends with what corresponded to a Reynolds number of 352,000.
  • the conversion of benzene in the diphenyl was 4.5% with a yield of 96% and there was no indication of carbon deposit.
  • Example VII The same tube used in Example VI was used at a constant temperature of 700 C. with the flow through the tube taking place in 1.17 seconds and a Reynolds number of 680,000. With each passage of the vapor through the tube 3.4% of the benzene was converted into diphenyl giving a yield of 96.5%. The daily production of diphenyl was 7.5 tons, which meant that 105 grams of diphenyl per hour per liter of capacity of the reaction tube takes place. There was no indication of carbon deposit.
  • Example VIII In this case, the pyrolysis tube was meters long and 77 mm. diameter. It was used with a temperature of 550 C. at the inlet and 800 C. at the outlet, this being a mean temperature of 680 C. The benzene vapor remained within the tube for 1.32 seconds (as in Example I) and the Reynolds number was 120,000. The conversion of benzene into diphenyl was 8.8% with each pass and a yield of 92%. Daily production was 1.33 tons which meant that 236 grams per hour, per liter of the capacity of the tube took place. No carbon was deposited on the inside surfaces of the tube.
  • Example V Diphenyl was produced in a reaction tube, diameter of which was mm. and the length 35 the internal meters. 75 to a pressure of 1.2 kgs. per centimeter squared.
  • a pressure is used of from 0.4 to 1.4 kgs. per centimeter squared and more often than not 0.9 to 1.2 kgs. per centimeter squared are used in addition to the atmospheric pressure at the inlet in the pipe 22 of the pyrolysis tube 2e.
  • there is a certain loss of head within the tube depending on the form and size of the latter. For example, when two tons of diphenyl are produced at 770 C. within a tube 76 meters long and 115 mm. in diameter with 18 bends, the loss of head is from 0.4 to 0.5 kg. per centimeter squared.
  • the apparatus of the invention is particulary useful for such pyrolyzing operations as the non-catalytic cracking of aliphatic hydrocarbons, alcohols, or other organic compounds and especially that of the arylic hydrocarbons; for example, in the production of diphenyl, terphenyls and other polyphenyls.
  • the special apparatus as suggested by the present invention preferably uses the tube of inner diameter between 55 and 205 mm., the size will be determined, to a certain extent, by the desired hourly production.
  • the length of the tube can be determined according to the specific process, but experience shows that industrial production demands the use of tubes having a length of from 30 to 100 meters and, particularly, those in the range of from 45 to meters.
  • the bends of the tube of the apparatus of the invention have their radii of curvature as little as possible compatible with the diameter of the tube. It is preferable, as has been stated, that the radius measured along the axis of the tube is of the same order as the external diameter of the tube, good results being obtained with radii equal to 1 to 2 times the said diameter. At the same time, it is important that the straight parts of the tube adjacent to the same bend make with respect to each other an angle as close as possible to zero degrees, and in any case, an angle of less than 30. However, angles of less than 17 are most advisable.
  • Apparatus for pyrolyzing benzene vapors or the like comprising a housing of cylindrical conformation, a heatexchange tube mounted within the housing having an internal diameter in the range from 55 to 205 mm. and a length in the range from 30 to meters, the tube being arranged in a sinuous conformation along the surface of an imaginary cylinder concentric with the housing, the tube consisting of U-shaped bends joined by straight portions lying along the generatrices of the imaginary cylinder, the radius of each bend being in the order of the outside diameter or" the tube so that the straight portions are spaced a distance apart approximately equal to the outside diameter of the tube, means for heating the interior of the housing, including an insulated wall surrounding the housing and carrying heating elements, and a pump bringing about a flow of vapor through the tube with a turbulence having a Reynolds number in the range from 120,000 to 500,000 with a residence time of the vapor in the tube in the range from 0.4 to 1.5 seconds at a temperature at the entrance in the range from 550 C. to

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US388346A 1960-12-06 1964-08-04 Apparatus for pyrolyzing vapors Expired - Lifetime US3227525A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FR846000A FR1299516A (fr) 1960-12-06 1960-12-06 Fabrication de diphényle

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US3227525A true US3227525A (en) 1966-01-04

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US (1) US3227525A (fr)
BE (1) BE611148A (fr)
CH (1) CH397618A (fr)
ES (1) ES272104A1 (fr)
FR (1) FR1299516A (fr)
GB (2) GB1003719A (fr)
NL (1) NL272200A (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070028984A1 (en) * 2003-03-18 2007-02-08 Imperial College Innovations Limited Helical piping
US20070157985A1 (en) * 2003-03-18 2007-07-12 Imperial College Innovations Limited Tubing and piping for multiphase flow
US20080017550A1 (en) * 2004-09-21 2008-01-24 Caro Colin G Piping
WO2007104952A3 (fr) * 2006-03-10 2008-03-13 Heliswirl Technologies Ltd Canalisation
US20080257436A1 (en) * 2004-09-21 2008-10-23 Caro Colin G Piping
US20090095594A1 (en) * 2004-09-21 2009-04-16 Heliswirl Technologies Limited Cracking furnace
US8354084B2 (en) 2008-09-19 2013-01-15 Technip France S.A.S. Cracking furnace

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2925377A (en) * 1955-04-01 1960-02-16 Exxon Research Engineering Co Isothermal catalytic reforming

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2925377A (en) * 1955-04-01 1960-02-16 Exxon Research Engineering Co Isothermal catalytic reforming

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090044954A1 (en) * 2003-03-18 2009-02-19 Caro Colin G Method for Transporting Multiphase Fluids
US20070157985A1 (en) * 2003-03-18 2007-07-12 Imperial College Innovations Limited Tubing and piping for multiphase flow
US20070028984A1 (en) * 2003-03-18 2007-02-08 Imperial College Innovations Limited Helical piping
US20090218037A1 (en) * 2003-03-18 2009-09-03 Caro Colin G Piping
US7749462B2 (en) 2004-09-21 2010-07-06 Technip France S.A.S. Piping
US20080257436A1 (en) * 2004-09-21 2008-10-23 Caro Colin G Piping
US20090095594A1 (en) * 2004-09-21 2009-04-16 Heliswirl Technologies Limited Cracking furnace
US20090235850A1 (en) * 2004-09-21 2009-09-24 Heliswirl Technologies Limited Piping
US20080017550A1 (en) * 2004-09-21 2008-01-24 Caro Colin G Piping
US8029749B2 (en) 2004-09-21 2011-10-04 Technip France S.A.S. Cracking furnace
US8088345B2 (en) 2004-09-21 2012-01-03 Technip France S.A.S. Olefin production furnace having a furnace coil
USRE43650E1 (en) 2004-09-21 2012-09-11 Technip France S.A.S. Piping
WO2007104952A3 (fr) * 2006-03-10 2008-03-13 Heliswirl Technologies Ltd Canalisation
EA014787B1 (ru) * 2006-03-10 2011-02-28 Хелисвирл Текнолоджиз Лимитед Трубопровод
US8354084B2 (en) 2008-09-19 2013-01-15 Technip France S.A.S. Cracking furnace

Also Published As

Publication number Publication date
BE611148A (fr)
GB1003719A (en) 1965-09-08
ES272104A1 (es) 1962-06-01
FR1299516A (fr) 1962-07-27
NL272200A (fr)
GB1003720A (en) 1965-09-08
CH397618A (fr) 1965-08-31

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