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Publication numberUS2119350 A
Publication typeGrant
Publication dateMay 31, 1938
Filing dateSep 13, 1935
Priority dateSep 22, 1934
Publication numberUS 2119350 A, US 2119350A, US-A-2119350, US2119350 A, US2119350A
InventorsDonath Ernst, Pier Mathias
Original AssigneeIg Farbenindustrie Ag
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Cracking of liquid hydrocarbon products
US 2119350 A
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Description  (OCR text may contain errors)

May 31, 1938. M. PIER ET AL 2,119,350

CRACKING OF LIQUID HYDROCARBON PRODUCTS Filed Sept. 15. 19:55

a Z FREJH OIL CATALYST STIRRING DEV/CE REACTION JTABILIZING. "mas/=1 CONDENSER HEAVY 01L .sEPARAToR PUMP CONUEMSER MIDDLE OIL A NH L IGH T OIL Mathias PzLer Zrns 2f Don/oath,

jwvenivn-s i W W Patented May 31, 1938 PATENT OFFICE 2,119,350 CRACKING or LIQUID maoonmor: rnonoc'rs Mathias Pier, Heidelberg, and Ernst Donath,

Mannheim, Germany, minors to I. G. Farbenindustrie Aktiengesellschatt, Frankfort-onthe-Main, Germany Application September .13, 1935, Serial No. 40,409 In Germany September 22, 1934 1 Claim.

The present invention relates to the cracking of liquid hydrocarbon products in the presence of catalysts.

In the cracking of liquid hydrocarbon prod 5 ucts (which expression also includes mixtures of liquid hydrocarbons with solid substances, as for example distillation residues), in particular of those hydrocarbon products which are rich in asphalts and unsaturated compounds, such as olefinic hydrocarbons, in the presence of catalysts,

' the activity of the latter is often impaired by the constituents having a high molecular weight of the nature of asphaltic andv resinous bodies which are present in the initial material and/or are formed during the reaction. We have now found that in the working up of the said hydro carbon products rich in asphalts and unsaturated hydrocarbons, i. e., products containing more than 4 per cent and usually more than 5 per cent of asphalts, this drawback can be overcome by carrying out the reaction in the presence of from 20 to 40 per cent of carbonaceous materials which under the reaction conditions are liquid and remain substantially undecomposed. Suitable carbonaceous materials are for example anthracene oil or aromatic heavy oils (usually boiling above 350 C.) which are free from asphalts and are derived, for example, from cracking or destructive hydrogenation processes carried through at high temperatures, as for example of 500 C. or more. As a rule use is made of those cyclic compounds which are practically free from asphaltic and resinous substances as well as from unsaturated aliphatic hydrocarbons. The said carbonaceous materials may be added to the material to be treated either prior to or during the cracking process. The amount of the carbonaceous material to be added depends on the nature of the initial material.

As initial materials for the cracking come into question, for example mineral oils or tars and the high boiling products obtained therefrom by distillation, cracking or destructive hydrogenation or the residues resulting from these processes. Middle oils of any origin are also suitable. These initial materials are subjected to cracking by heating to from 400 to 700 C. in the presence of a catalyst having a splitting action. Especially when employing high-boiling initial materials it has proved useful to add these catalysts while in a finely dispersed form, in which the single particles have a size of about from 0.01 to 0.06 millimetre or less. As catalysts come into question metals, in particular those of the 1st to the 4th and the 8th groups, as for examplecopper, zinc, aluminium, silicon, titanium, thorium, iron, as well as vanadium or chromium, or the compounds of these metals, as for example the oxides and halides, such as bauxite or other known catalysts having a splitting action on hydrocar- 5 bons. The catalytically active metals or metal compounds may also be applied to carriers, such as active carbon, coke, llgnite coke and the like. When the catalyst is employed in a finely divided form, it is of advantage to add it in small 10 amounts, as for example of from 0.5 to 5 per cent. The catalyst is then led, in conjunction with the initial material, through the cracking apparatus and afterwards removed from the reaction product.

Besides, there may also be added halogen or metal halides or, with particular success organic halogen compounds, such as carbon tetrachloride, ethylene dichloride, chloroform, benzoylchloride and the likB. The process may be effected by means of an apparatus such as is depicted diagrammatically in the accompanying drawing.

On the drawing: Reference numeral l indicates a hopper from 25 -which catalyst is fed to vessel 3 by means of of hot combustion gases, coil 8 discharging into 35 the reaction vessel 9. The products of the reaction escape from the reaction vessel through line 10 and, after passing through condenser II, are discharged into the heavy oil separator I2. The uncondensed gases and vapors escape from 4,0 separator I! through line l2a and pass via condenser iii to the collecting vessel It. The gases leave the collecting vessel I4 by means of pipe I 5. The heavy oil which collects in vessel I! may be supplied by means of pump it and line 45 I1 to the mixing vessel 5.

The following example serves to illustrate how the present invention may be carried out in practice, but the invention is not restricted to this example. 50

Example A mineral oil distillation residue which boils above 325 0., is mixed with 20 per cent of its weight of anthracene oil and 1 per cent of a 55 vessel.

finely divided activated lignite coke impregnated with a solution containing iron chloride and nickel chloride. The mixture is then heated up to 470 C. in a tubular system heated with combustion gases, the pressure maintained in the tubes being atmospheres, whereupon the heated mixture is led into an enlarged reaction The reaction product issuing from this vessel contains 32 per cent of benzine besides the anthracene oil which is practically unchanged. The anthracene oil is recovered by distillation in vacuo and then employed again as additional substance.

I! the reaction is carried out without an addition of anthracene oil the yield of benzine is considerably smaller and the operation must be interrupted after a short period due to the separation of coke in the apparatus.

What we claim is:-

In a process for cracking liquid hydrocarbon products boiling above 325 0., rich in polymerizable unsaturated hydrocarbons and containing more than 4% of asphalt in the presence of solid catalysts havinga splitting action, the particles of said catalyst having a size less than .06 mm. and in the absence of any substance tending to depress the formation of resinous products, the improvement which comprises avoiding a poisoning of the catalyst by any asphalt and resinous constituents present in the parent materials and formed during the reaction, by heating such products to a cracking temperature within the range of 400 to 700 C. while in admixture with from about 20 to 40% of a substantially aromatic heavy oil boiling above 350' 0., which eil'ects dissolution of said asphalt and resinous constituents, said oil remaining undecomposed at the cracking temperature selected.

MA'I'HIAB PIER.

ERNST DONATH.

Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2897133 *Jun 25, 1954Jul 28, 1959Union Oil CoHydrocarbon treatment process and apparatus
US5110443 *Apr 18, 1989May 5, 1992Canadian Occidental Petroleum Ltd.Converting heavy hydrocarbons into lighter hydrocarbons using ultrasonic reactor
Classifications
U.S. Classification208/125, 502/181, 422/659
International ClassificationC10G53/08
Cooperative ClassificationC10G53/08
European ClassificationC10G53/08