DE1107216B - Process for the cleavage of high-boiling hydrocarbon oils - Google Patents
Process for the cleavage of high-boiling hydrocarbon oilsInfo
- Publication number
- DE1107216B DE1107216B DEB56072A DEB0056072A DE1107216B DE 1107216 B DE1107216 B DE 1107216B DE B56072 A DEB56072 A DE B56072A DE B0056072 A DEB0056072 A DE B0056072A DE 1107216 B DE1107216 B DE 1107216B
- Authority
- DE
- Germany
- Prior art keywords
- hydrocarbon oils
- boiling hydrocarbon
- cleavage
- solids
- boiling
- 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.)
- Pending
Links
- 238000009835 boiling Methods 0.000 title claims description 10
- 238000000034 method Methods 0.000 title claims description 10
- 229930195733 hydrocarbon Natural products 0.000 title claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 7
- 239000003921 oil Substances 0.000 title claims description 6
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 5
- 238000003776 cleavage reaction Methods 0.000 title description 2
- 230000007017 scission Effects 0.000 title description 2
- 239000007787 solid Substances 0.000 claims description 9
- 239000010779 crude oil Substances 0.000 description 5
- 150000001336 alkenes Chemical class 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000007858 starting material Substances 0.000 description 3
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 229910052851 sillimanite Inorganic materials 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000004992 fission Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
-
- 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
- C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
- C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
Das Hauptpatent 1 083 805 betrifft ein Verfahren zur Spaltung von hochsiedenden Kohlenwasserstoffölen an erhitzten feinzerteilten Feststoffen zur Herstellung von niedrigsiedenden Olefinen aus Rohöl, bei dem man die Dämpfe der unter 350 bis 500° C siedenden Bestandteile des zu spaltenden Öles gegebenenfalls in Gegenwart von anderen Trägergasen mit Feststoffen, die in einer ersten Wirbelschicht auf 900 bis 1200° C erhitzt wurden, durch eine als Steigleitung ausgebildete Reaktionszone führt, die dabei durch Spaltung bei Temperaturen von 730 bis 950° C entstandenen Gase in einer Trennvorrichtung von den Feststoffen abtrennt, die Feststoffe einer zweiten Wirbelschicht zuleitet, in der bei Temperaturen von 650 bis 800° C der nicht oder schwer verdampfbare Rückstand des Ausgangsstoffes gespalten wird, die dabei entstandenen Gase von mitgeführten Feststoffen abtrennt und diese durch eine zweite Steigleitung unter Verwendung von Trägergasen in die erste Wirbelschicht zurückführt.The main patent 1 083 805 relates to a process for the cleavage of high-boiling hydrocarbon oils of heated, finely divided solids for the production of low-boiling olefins from crude oil from which the vapors of the constituents of the oil to be split which boil below 350 to 500 ° C, if necessary in the presence of other carrier gases with solids, which in a first fluidized bed to 900 were heated to 1200 ° C, through a reaction zone designed as a riser, which leads thereby gases formed by splitting at temperatures of 730 to 950 ° C in a separator from the Separates solids, the solids fed to a second fluidized bed in which at temperatures of 650 to 800 ° C the non-evaporable or difficult to evaporate residue of the starting material is split, the The resulting gases are separated from entrained solids and these are separated through a second riser returned to the first fluidized bed using carrier gases.
Das Verfahren eignet sich besonders zur Herstellung von niedrigsiedenden Olefinen aus Rohölen, insbesondere mit einem möglichst hohen Anteil an Äthylen.The process is particularly suitable for the production of low-boiling olefins from crude oils, in particular with the highest possible proportion of ethylene.
Es wurde nun gefunden, daß man den gesamten Anteil der im Reaktionsprodukt enthaltenen Olefine erhöhen kann, wenn man die Feststoffe der ersten Wirbelschicht auf Temperaturen von 750 bis 900° C erhitzt.It has now been found that the total proportion of olefins contained in the reaction product can be increased can, if the solids of the first fluidized bed to temperatures of 750 to 900 ° C heated.
Diese Abänderung des Verfahrens nach dem Hauptpatent hat noch den weiteren Vorteil, daß, wie in vielen Fällen gewünscht, der Anteil der Olefine mit mehr aus 2 Kohlenstoffatomen, insbesondere der Anteil an Propylen, vergrößert wird. Nach dem Verfahren können die gleichen Ausgangsstoffe wie bei dem Verfahren des Hauptpatents umgesetzt werden, z. B. neben Rohölen hochsiedende Kohlenwasserstofföle oder bestimmte Rohölfraktionen, die hochsiedende Bestandteile enthalten.This modification of the process according to the main patent has the further advantage that how in many cases desired, the proportion of olefins with more than 2 carbon atoms, in particular the Proportion of propylene, is increased. After the process, the same starting materials as for the process of the main patent are implemented, e.g. B. In addition to crude oils, high-boiling hydrocarbon oils or certain crude oil fractions that contain high-boiling components.
Das Verfahren wird nach den Angaben des Hauptpatents ausgeführt, lediglich mit der Abänderung, daß die Feststoffe in dem dafür vorgesehenen Wirbelbett auf 750 bis 900° C erhitzt werden, bevor sie zusammen mit den unterhalb 350 bis 500° C siedenden Bestandteilen des Ausgangsstoffes, gegebenenfalls zusammen mit erhitztem Wasserdampf, in der als Reaktionsrohr dienenden Steigleitung nach oben befördert und dabei durch Erhitzen auf 730 bis 950° C gespalten werden.The procedure is carried out according to the information in the main patent, only with the amendment that the solids are heated to 750 to 900 ° C in the fluidized bed provided before they are put together with the constituents of the starting material boiling below 350 to 500 ° C, if necessary conveyed upwards in the riser pipe serving as a reaction tube together with heated steam and are split by heating to 730 to 950 ° C.
Die übrigen Reaktionsbedingungen bleiben ganz im Rahmen der Ausführungen im Hauptpatent. Es können auch dieselben Feststoffe verwendet werden.The other reaction conditions remain entirely within the scope of the statements in the main patent. It the same solids can also be used.
Verfahren zur Spaltung von
hochsiedenden KohlenwasserstoffölenProcedure for splitting
high-boiling hydrocarbon oils
Zusatz zum Patent 1 083 805Addendum to patent 1,083,805
ίο Anmelder:ίο applicant:
Badische Anilin- & Soda-FabrikAniline & Soda Factory in Baden
Aktiengesellschaft,
Ludwigshafen/RheinCorporation,
Ludwigshafen / Rhine
Dr. Heinz Engelbach, Ludwigshafen/Rhein,
ist als Erfinder genannt wordenDr. Heinz Engelbach, Ludwigshafen / Rhine,
has been named as the inventor
Die Durchführung des Verfahrens erfolgt beispielsweise in einer Apparatur, wie sie in der Abbildung wiedergegeben wird.The process is carried out, for example, in an apparatus as shown in the figure is reproduced.
Beispiel
30example
30th
1000 kg/h eines vorwiegend aus paraffinischen Kohlenwasserstoffen bestehenden Rohöls werden in einer Anlage, die in der Abbildung wiedergegeben ist, destillativ bei 280° C in 350 kg Destillat und 650 kg Rückstand zerlegt. Die Dämpfe des Destillats strömen zusammen mit 160 kg/h überhitztem Wasserdampf über Stutzen 16 in das Steigrohr 17. Gleichzeitig werden aus dem Fallrohr 11 etwa 24 t/h Sillimanit von 0,3 bis 2,0 mm Korngröße durch den Dosiergasstrom aus Leitung 15 dem unteren Ende des Steigrohres 17 zugeführt. Die Wärmeträgerteilchen werden von den durch Rohr 16 eintretenden Dämpfen in den Zyklon 18 gefördert, die wegen der im Steigrohr erfolgenden innigen Durchmischung rasch auf Spalttemperatur erhitzt werden. Der Sillimanit, der im Heizofen 1 auf etwa 865° C erhitzt wird, kühlt sich, während er im Steigrohr 17 gehoben wird, bis auf etwa 800° C ab. Er wird im Zyklon 18 abgeschieden und fließt über Rohr 19 der Wirbelschicht des Spaltofens 2 zu, die durch 320 kg/h überhitzten Wasserdampf (Rohrstutzen 21) aufgewirbelt wird, wobei sich eine Spalttemperatur von etwa 720° C einstellt. Die1000 kg / h of a crude oil consisting predominantly of paraffinic hydrocarbons are used in a plant, which is shown in the figure, by distillation at 280 ° C in 350 kg of distillate and 650 kg Disassembled residue. The vapors of the distillate flow together with 160 kg / h of superheated steam Via nozzle 16 into the riser pipe 17. At the same time, about 24 t / h of sillimanite are produced from the downpipe 11 0.3 to 2.0 mm grain size through the metering gas flow from line 15 to the lower end of the riser pipe 17 supplied. The heat transfer particles are absorbed by the vapors entering through pipe 16 in the Cyclone 18 promoted, which due to the intimate mixing taking place in the riser pipe quickly to the gap temperature be heated. The sillimanite, which is heated to around 865 ° C in heating furnace 1, cools down, while it is lifted in the riser pipe 17, down to about 800 ° C. It is separated in cyclone 18 and flows through pipe 19 to the fluidized bed of the cracking furnace 2, the steam superheated by 320 kg / h (Pipe socket 21) is whirled up, a gap temperature of about 720 ° C being established. the
1B9 608/4291B9 608/429
vereinigten Spaltgase werden nach Verlassen des Zyklons 18 auf etwa 200° C abgeschreckt und in üblicher Weise aufgearbeitet. Man erhält 242 kg Äthylen, 142 kg Propylen, 74 kg ungesättigte C4- und Cg-Kohlenwasserstoffe und 141 kg bis etwa 180° C siedende aromatische Kohlenwasserstoffe in der Stunde.The combined fission gases are quenched to about 200 ° C. after leaving the cyclone 18 and worked up in the usual way. 242 kg of ethylene, 142 kg of propylene, 74 kg of unsaturated C 4 and Cg hydrocarbons and 141 kg of aromatic hydrocarbons boiling up to about 180 ° C. are obtained per hour.
Claims (1)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEB56072A DE1107216B (en) | 1959-12-29 | 1959-12-29 | Process for the cleavage of high-boiling hydrocarbon oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEB56072A DE1107216B (en) | 1959-12-29 | 1959-12-29 | Process for the cleavage of high-boiling hydrocarbon oils |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| DE1107216B true DE1107216B (en) | 1961-05-25 |
Family
ID=6971203
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DEB56072A Pending DE1107216B (en) | 1959-12-29 | 1959-12-29 | Process for the cleavage of high-boiling hydrocarbon oils |
Country Status (1)
| Country | Link |
|---|---|
| DE (1) | DE1107216B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1222038B (en) | 1960-03-16 | 1966-08-04 | Basf Ag | Process for the splitting of hydrocarbons into gaseous olefins |
-
1959
- 1959-12-29 DE DEB56072A patent/DE1107216B/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1222038B (en) | 1960-03-16 | 1966-08-04 | Basf Ag | Process for the splitting of hydrocarbons into gaseous olefins |
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