EP0499897B1 - Contrôle des processus dans les fours de pyrolyse pour la préparation d'oléfines - Google Patents

Contrôle des processus dans les fours de pyrolyse pour la préparation d'oléfines Download PDF

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Publication number
EP0499897B1
EP0499897B1 EP92102007A EP92102007A EP0499897B1 EP 0499897 B1 EP0499897 B1 EP 0499897B1 EP 92102007 A EP92102007 A EP 92102007A EP 92102007 A EP92102007 A EP 92102007A EP 0499897 B1 EP0499897 B1 EP 0499897B1
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zone
steam
mixed
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EP92102007A
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German (de)
English (en)
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EP0499897A1 (fr
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Heinz. Dr.-Ing. Zimmermann
Wolfgang Schwab
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Linde GmbH
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Linde GmbH
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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

Definitions

  • the invention relates to a method for controlling the transition temperature between the convection and the radiation zone in cracking furnaces for olefin production from different hydrocarbon inserts.
  • the required high temperatures in the cracking zone are usually achieved by passing the feed material through cracked tubes which are arranged in the radiation zone of a burner-heated cracking furnace.
  • the hot flue gases generated during the firing form a large heat reservoir after exiting the radiation zone, which can be used to preheat the use of hydrocarbons and possibly other fluids and for this purpose is passed through a convection zone equipped with heat exchangers.
  • DE-A-15 68 966 teaches what such a regulation can look like. It relates to a control method for the splitting of hydrocarbons, in which the transition temperature between a convection part and a radiation part of a cracking furnace is regulated by either part of the hot flue gases or part of the hydrocarbons to be preheated being circulated around the convection zone.
  • the known method is aimed at influencing the temperature profile within a can which penetrates a convection zone and a subsequent radiation zone.
  • a greater steepness of the temperature profile in the radiation zone is achieved in that the preheating of the gap insert in the convection zone is reduced, so that the transition temperature from the convection zone to the radiation zone is reduced and preheating is initially continued in the radiation zone.
  • An essential aspect of this method is to be seen in the fact that the regulation provided there works in such a way that the predetermined end temperature T E is reached at the outlet end of the can.
  • the cited German published application does not indicate any changes to the procedure to be undertaken in the event of a transition to a completely different gap insert, for example the transition from gasoline fractions to gas oil.
  • transition temperature also called cross-over temperature
  • the present invention is therefore based on the object of developing a method of the type mentioned above in such a way that it is possible to adapt the transition temperature between the convection and radiation zones in the most varied of hydrocarbon applications in a process-technically simple manner and with an improved economy of the process sequence.
  • This object is achieved in that the feed stream is divided into two sub-streams before being introduced into the convection zone, the first sub-stream initially preheated, then mixed with process steam, then mixed with the second, up to this point in time untreated partial stream and the total process stream thus formed is led into the radiation zone after further heating and / or evaporation.
  • One embodiment of the method according to the invention is to overheat the process steam before it is mixed with the first partial stream.
  • This process steam superheating can take place on the one hand in a heat exchanger in the convection zone of the cracking furnace for hot flue gas coming from the radiation zone of the cracking furnace, and on the other hand in any manner outside the cracking furnace.
  • the former embodiment is used above all in the case of liquid hydrocarbon inserts, since only partial evaporation of the first partial stream takes place here, and only when the superheated process steam and the first partial stream are mixed does an almost complete evaporation take place due to the heat released by the superheated process steam onto the hydrocarbons.
  • a further embodiment of the method according to the invention provides the possibility of initially mixing the process steam and the first partial stream and then feeding the gas mixture thus formed to a heat exchanger where it is heated to such an extent that the gas mixture overheats.
  • a further embodiment of the method according to the invention discloses the possibility of preheating the first partial stream in one or more stages before mixing with process steam.
  • the heating of the overall process stream formed after the mixing of the two partial streams can take place in one or more steps.
  • a further embodiment of the method according to the invention consists in preheating the first partial stream and further heating the overall process stream formed after the two partial streams have been mixed by indirect heat exchange with the hot flue gas coming from the radiation zone.
  • the process according to the invention is applicable to hydrocarbon inserts as diverse as ethane, propane, butane, liquid gas, naphtha, kerosene, atmospheric gas oil, hydrogenated atmospheric gas oil and hydrogenated vacuum gas oil.
  • hydrocarbon inserts as diverse as ethane, propane, butane, liquid gas, naphtha, kerosene, atmospheric gas oil, hydrogenated atmospheric gas oil and hydrogenated vacuum gas oil.
  • the method according to the invention now allows a relatively inexpensive adaptation of the splitting process to a wide variety of hydrocarbon uses. This enables an optimized and thus maximum utilization of the hydrocarbon feedstocks with the lowest possible energy consumption, specifically heating gas for operating the burners in the radiation zone and the resulting quantity and temperature of the flue gas.
  • the constructional and operational expenditure compared to the cited prior art can be significantly reduced.
  • the method according to the invention thus reduces the investment and operating costs on the basis of the following improvements: Optimization of the utilization at different Hydrocarbon inserts, minimization of the heating media required and constructional simplification of the convection zone of a cracking furnace for olefin production from different hydrocarbon inserts.
  • Precise control of the transition temperature between the convection and radiation zones also enables the reduction of coke deposits in the heat exchanger through which the entire process gas flow last flowed.
  • the rate of coking of the gas lines essentially depends both on the temperature of the gas mixture to be split and on the cracking severity. This means that the start of the actual fission processes in the last heat exchangers of the convection zone should be avoided. Rapid coking of the gas lines can drastically shorten the life of a cracking furnace.
  • the regulation of the transition temperature now makes it possible to set a temperature which is chosen for each hydrocarbon used in such a way that coking does not yet take place in the convection zone.
  • the avoidance of operational interruptions due to decoking work in the convection zone leads to an improvement in the economy of the cracking furnace.
  • Figure 1 is the basic representation of the method according to the invention. It shows the convection zone of a cracking furnace for the thermal decomposition of different hydrocarbon inserts.
  • the hydrocarbon feed stream is led via line 1 upstream of the convection zone and divided into a first partial stream (line 2) and a second partial stream (line 3) in the desired ratio.
  • the first partial flow is then fed via line 2 to a heat exchanger B, heated against cooling flue gas (represented by the dashed arrows) from the radiation zone of the cracking furnace and discharged via line 2a.
  • the process steam required for diluting the hydrocarbon feed is fed to a heat exchanger C via line 4 and overheated in it against cooling flue gas.
  • the superheated process steam is then drawn off via line 4a, mixed with the heated first partial stream from line 2a and brought together via line 2c with the second, previously untreated partial stream in line 3.
  • the total process stream thus formed is then fed via line 5 to a heat exchanger D, where it is further heated or evaporated against cooling flue gas.
  • a heat exchanger D After bypassing an intermediate heat exchanger E, which will be described below, the total process stream is fed via line 6 to a last heat exchanger F in the convection zone and heated in it against cooling hot flue gas to the desired transition temperature between the convection and radiation zones before being conducted via line 7 is directed into the radiation zone.
  • feed water supplied via line 10 is heated and then passed via line 11 into a high-pressure steam drum, not shown here.
  • This feed water serves as a coolant for the quenching of the cracked gases, for which purpose it is fed to a quench cooler.
  • steam is formed, which is collected in the upper area of the quench cooler and returned to the steam chamber of the high-pressure steam drum. From there it passes via line 12 into the heat exchanger E, where it is overheated against high-temperature flue gas.
  • the superheated steam is drawn off via line 13 and can be used, for example, to operate a turbine for energy recovery.
  • the flue gas has a temperature of 1000 ° C to 1200 ° C at the transition from the radiation to the convection zone, leaves the convection zone shown here at the upper end with a temperature of about 130 ° C and is removed via a chimney, if necessary after cleaning .
  • FIG. 2 shows a further embodiment of the method according to the invention.
  • the hydrocarbon feed is divided into a first partial stream (line 2) and a second partial stream (line 3) in the desired ratio.
  • the first partial stream is fed via line 2 into a heat exchanger B, heated against cooling flue gas and drawn off via line 2a.
  • Process steam required for dilution is introduced via line 4 and mixed with the first, already heated partial flow in line 2a, the gas mixture thus formed is fed via line 2b to a further heat exchanger C and heated in it to such an extent that the process steam component overheats.
  • the gas mixture is then over Line 2c withdrawn and mixed with the second, up to this point in time untreated stream in line 3.
  • the total process stream formed in this way is conducted analogously to FIG. 1 via lines 5, 6 and 7 and heat exchangers D and F into the radiation zone.
  • Points 21 and 22 each indicate a measuring point for flow rate control in the two partial streams in line 2 and line 3.
  • Points 23 to 28 indicate six temperature measuring points.
  • Table 1 shows the range in which the transition temperature, which corresponds to the temperature of the measuring point 28, can be varied. Ethane is chosen as the hydrocarbon feed.
  • Gas oil at a pressure of 5.4 bar and a temperature of 82 ° C. is supplied in liquid form via line 1 and 2 to heat exchanger B. After heating to 357 ° C, half of the gas oil which has already evaporated is drawn off at a pressure of 5.4 bar via line 2a.
  • Heat exchanger C water vapor is supplied via line 4 at a pressure of 5.6 bar and a temperature of 179.degree. After overheating, the water vapor is drawn off at a pressure of 5.4 bar and a temperature of 449 ° C. via line 4a and mixed with the gas oil from line 2a. The mixing results in a complete evaporation of the mixture formed, so that a mixture with a pressure of 5.0 bar and a temperature of 361 ° C.
  • feed water is preheated in heat exchanger A from 110 ° C to 140 ° C and superheated steam in heat exchanger E from 329 ° C to 527 ° C.
  • the hot flue gas has a temperature of 1124 ° C when entering the convection zone and leaves the convection zone after overflowing the seven heat exchangers A to F at a temperature of 122 ° C.
  • Gaseous ethane with a pressure of 3.9 bar and a temperature of 68 ° C. is introduced via line 1 as the hydrocarbon feed. 30% of the feed are fed via line 2 to heat exchanger B, heated to 646 ° C. in it and discharged via line 2a at a pressure of 3.9 bar.
  • Heat exchanger C steam at a pressure of 3.9 bar and a temperature of 175 ° C., is fed in via line 4, overheated to 629 ° C., drawn off via line 4a at constant pressure and mixed with the heated ethane from line 2a.
  • the gas mixture formed is brought together via line 2c with the remaining 70% of the hydrocarbon feed which has hitherto been untreated, and the mixture thus formed is fed via line 5 to heat exchanger D at a pressure of 3.5 bar and a temperature of 347 ° C. It is further heated to 496 ° C., whereupon the gas mixture is fed into the heat exchanger F via line 6 at a pressure of 3.4 bar. Here it heats up to a transition temperature of 649 ° C before the mixture reaches the radiation zone via line 7.
  • feed water is preheated or evaporated in heat exchanger A from 110 ° C to 309 ° C and superheated steam in heat exchanger E from 330 ° C to 504 ° C.
  • the hot flue gas has a temperature of 1182 ° C when entering the convection zone and leaves the convection zone after overflow of the seven heat exchangers A to F at a temperature of 183 ° C.
  • Gaseous ethane with a pressure of 4.0 bar and a temperature of 68 ° C. is introduced via line 1 as the hydrocarbon feed. 60% of the feed are fed via line 2 to heat exchanger B, heated to 643 ° C. in it and discharged via line 2a at a pressure of 3.9 bar. Heat exchanger C, steam at a pressure of 3.9 bar and a temperature of 175 ° C., is fed in via line 4, overheated to 636 ° C., drawn off via line 4a at constant pressure and mixed with the heated ethane from line 2a.
  • the gas mixture formed is brought together via line 2c with the remaining 40% of the hydrocarbon feed which has hitherto been untreated, and the mixture thus formed is fed via line 5 to heat exchanger D at a pressure of 3.5 bar and a temperature of 482 ° C. It is heated further to 581 ° C., whereupon the gas mixture is fed into the heat exchanger F via line 6 at a pressure of 3.5 bar. Here it is heated to a transition temperature of 709 ° C before the mixture reaches the radiation zone via line 7.
  • feed water is preheated or evaporated in heat exchanger A from 110 ° C to 256 ° C and superheated steam in heat exchanger E from 329 ° C to 527 ° C.
  • the hot flue gas has a temperature of 1166 ° C when entering the convection zone and leaves the convection zone after overflow of the seven heat exchangers A to F at a temperature of 162 ° C.

Claims (9)

  1. Procédé de régulation de la température de transition entre la zone de convection et la zone de rayonnement dans des fours de craquage pour la production d'oléfines à partir de différentes charges d'hydrocarbures, caractérisé en ce que le courant de charge est divisé avant introduction dans la zone de convection en deux courants partiels, le premier courant partiel étant d'abord préchauffé, puis mélangé à la vapeur produite dans le procédé, et est mélangé enfin au second courant partiel, non-traité jusqu'alors, le courant global obtenu étant amené à la zone de rayonnement après réchauffage et/ou vaporisation ultérieur(s).
  2. Procédé selon la revendication 1, caractérisé en ce que la vapeur produite dans le procédé est surchauffée et mélangée ensuite au premier courant partiel.
  3. Procédé selon la revendication 2, caractérisé en ce que la vapeur produite dans le procédé est surchauffée dans un échangeur thermique de la zone de convection du four de craquage, au contact d'un gaz de combustion provenant de la zone de rayonnement du four de craquage.
  4. Procédé selon la revendication 2, caractérisé en ce que de la vapeur produite dans le procéde est amenée déja surchauffée à l'extérieur du four de craquage.
  5. Procédé selon la revendication 1, caractérisé en ce que le premier courant partiel et la vapeur produite sont d'abord mélanges puis réchauffés ensuite jusqu'à parvenir à une surchauffe du mélange de gaz obtenu.
  6. Procedé selon l'une des revendications 1 à 5, caractérisé en ce que le préchauffage du premier courant partiel est effectué en une ou plusieurs étapes avant le mélange avec la vapeur produite dans le procédé.
  7. Procédé selon l'une des revendications 1 à 6, caracterisé en ce que le réchauffage ultérieur du courant global obtenu formé après mélange des deux courants partiels peut s'effectuer en une ou plusieurs étapes.
  8. Procédé selon l'une des revendications 1 à 7, caractérisé en ce que le préchauffage ultérieur du courant global obtenu formé après mélange des deux courants partiels s'effectue par échange thermique indirect avec le gaz de combustion sortant de la zone de rayonnement.
  9. Procédé selon l'une des revendications 1 à 7, caractérisé en ce qu'on emploie commc charge d'hydrocarbures, de l'éthane, du propane, du butane, du gaz liquéfié, du naphta, du kérosène, du gazole de distillation atmosphérique, du gazole de distillation atmosphérique hydrogéné et du gazole de distillation sous vide hydrogené.
EP92102007A 1991-02-19 1992-02-06 Contrôle des processus dans les fours de pyrolyse pour la préparation d'oléfines Expired - Lifetime EP0499897B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT92102007T ATE98668T1 (de) 1991-02-19 1992-02-06 Verfahren zur prozesssteuerung in spaltoefen zur olefinherstellung.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4105095 1991-02-19
DE4105095A DE4105095A1 (de) 1991-02-19 1991-02-19 Verfahren zur prozesssteuerung in spaltoefen zur olefinherstellung

Publications (2)

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EP0499897A1 EP0499897A1 (fr) 1992-08-26
EP0499897B1 true EP0499897B1 (fr) 1993-12-15

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EP92102007A Expired - Lifetime EP0499897B1 (fr) 1991-02-19 1992-02-06 Contrôle des processus dans les fours de pyrolyse pour la préparation d'oléfines

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EP (1) EP0499897B1 (fr)
JP (1) JPH06116568A (fr)
AT (1) ATE98668T1 (fr)
DE (2) DE4105095A1 (fr)
MX (1) MX9200527A (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT398428B (de) * 1993-01-27 1994-12-27 Oemv Ag Vorrichtung zum thermischen spalten eines gemisches mit flüssigen und gasförmigen kohlenwasserstoffen
EP1727877B1 (fr) * 2004-03-22 2012-04-04 ExxonMobil Chemical Patents Inc. Procede de craquage vapeur de brut lourd
CN103003476B (zh) 2010-07-02 2016-02-10 宝洁公司 纤维网材料以及用于制造纤维网材料的方法
JP5859526B2 (ja) 2010-07-02 2016-02-10 ザ プロクター アンド ギャンブルカンパニー 活性剤不織布ウェブを含むフィラメント及びその製造方法
WO2012003367A2 (fr) 2010-07-02 2012-01-05 The Procter & Gamble Company Procédé de diffusion d'un agent actif
DE102012008038A1 (de) 2012-04-17 2013-10-17 Linde Ag Konvektionszone eines Spaltofens
JP7381613B2 (ja) 2019-06-28 2023-11-15 ザ プロクター アンド ギャンブル カンパニー アニオン性界面活性剤を含有する溶解性固体繊維性物品
MX2023001042A (es) 2020-07-31 2023-02-16 Procter & Gamble Bolsa fibrosa soluble en agua que contiene granulos para el cuidado del cabello.

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1568966A1 (de) * 1966-10-12 1970-07-16 Linde Ag Verfahren und Vorrichtung zur Prozesssteuerung in Spaltoefen fuer die thermische Spaltung von Kohlenwasserstoffen
DE2854061A1 (de) * 1978-12-14 1980-07-03 Linde Ag Verfahren zum vorwaermen von kohlenwasserstoffen vor deren thermischer spaltung
US4479869A (en) * 1983-12-14 1984-10-30 The M. W. Kellogg Company Flexible feed pyrolysis process

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DE59200031D1 (de) 1994-01-27
MX9200527A (es) 1992-08-01
ATE98668T1 (de) 1994-01-15
JPH06116568A (ja) 1994-04-26
DE4105095A1 (de) 1992-08-20
EP0499897A1 (fr) 1992-08-26

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