US2433030A

US2433030A - Separation of olefins from a hydrocarbon stream

Info

Publication number: US2433030A
Application number: US639608A
Authority: US
Inventors: John H Cone
Original assignee: Standard Oil Development Co
Current assignee: Standard Oil Development Co
Priority date: 1946-01-07
Filing date: 1946-01-07
Publication date: 1947-12-23
Anticipated expiration: 1964-12-23

Description

Dec. 23, 1947.

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Patented Dec. 23, 1947 SEPARATION OF OLEFINS FROM A HYDROCARBON STREAM John H. Cone Goose Creek, Tex., assignor to Standard Oil Development Company, a corporation of Delaware Application January 7, 1946, Serial No. 639,608

Claims. (01. 260-677) 1 The present invention is directed to a method for concentrating relatively weak sulfuric acid which previously has been employed for treating As an example of a typical operation, a hydrocarbon feed stock, including iso and normal butane, isobutylene and normal butylene, may be brought into contact with 65% sulfuric acid in a reaction zone under a pressure substantially in excess of atmospheric in order to form an extract. The pressure on this extract is reduced to substantially atmospheric in a vent drum with the resultant release of the butanes and normal butylenes previously absorbed therein. The extract is then sentpto a regenerator where polymers and alcohols resulting from the reaction of the sulfuric acid withTthe hydrocarbon mixture are separated as overhead fractions and the acid is concentrated to a 45% strength. The acid is removed from the regenerator to an acid con- 1 centrator where itsstrength is increased to 65% and then returned to the reaction-zone of the system. In conventional operations, substantial foaming is encountered in the vent drums, in the regenerator and in the acid concentrator and this foaming requires these portions of the system to be operated at a rate below that which may be employed when foaming is eliminated.

In accordance with the present invention, foaming in the vent drum, regenerator and acid concentrator is eliminated or greatly reduced by washing the extract with a naphthene hydrocarbon or a lubricating oil distillate from a naphthene base crude oil. The washing step removes foaming agents from the sulfuric acid extract and allows the extract to be sent through the vent drum, regeneratcr and acid concentrator with little or no foaming.

Naphthene hydrocarbons are well-known commercial products. The best known source of these hydrocarbons is petroleum, particularly petroleum produced from such sections as the Gulf 2 Coast, and California fields. The present invention may conveniently be practiced by employing a purified naphthene hydrocarbon recovered from petroleum by any of the conventional methods or, if desired, by using a naphthene base crude oil distillate having a viscosity in the range of about 20 to 500 seconds Saybolt viscosity at F. obtained by subjecting the crude oil to distillation. If desired, the distillate may be subjected to a purification process as by treatment with sodium hydroxide or other alkali metal hydroxide solution.

In accordance with the present invention, the sulfuric acid extract obtained by contacting the hydrocarbon mixture with sulfuric acid is Washed with a naphthene hydrocarbon or a lubricating oil distillate of about 20 to 500 Saybolt viscosity at 100 F. derived from a naphthene base crude oil to remove foam producing agents therefrom prior to the several steps employed for recovering the hydrocarbons from the sulfuric acid extract and for .reconcentrating the sulfuric acid. The step of washing the sulfuric acid extract with the naphthene hydrocarbon or naphthene base oil may be conducted either ,as a batch process or as a continuous process, and the amount of naphthene hydrocarbon or naphthene base oil employed may be varied over a wide range. be found convenient to wash the sulfuric acid extract with an amount of naphthene hydrocarbon or naphthene base oil in the range of 1 to 20 volume per cent. If desired, a charge of naphthene hydrocarbon or naphthene baseoil may be used a number of times for washing sulfuric acid extract. In order to co-ordinate the present invention with commercial refinery operations where continuous processes are employed wher-' ever possible, it will usually be desirable to conduct the process of the present invention as a continuous operation and recycle continuously the naphthene hydrocarbon or naphthene base oil used to wash the sulfuric acid extract. The naphthene or naphthene base oil employed for the washing step may be circulated a number of times through the washing step and then replaced by a new batch or, alternatively, 'a small portion of fresh naphthene or naphthene base oil added thereto and an equal portion of used naphthene or naphthene base oil removed therefrom continuously. J

*The invention will now be described in greater detail in onjunction with the drawing in which the singl ifigure is in the form of a flow sheet illustrating a preferred modification of the present invention.

It will In the drawing is shown a first stage reactor 9, a first stage settling drum I0, a-seco'nd stage reactor II, a second stage settling drum I2, a mixing device I3, a settling vessel I4, a vent drum l5, a regenerator vessel I6 and an acid concentrator vessel II. The mixture of said hydrocarbons is passed to the system from a storage vessel I8.

The system shown in the drawing may be described generally as involving a reaction zone, an acid regenerator zone, and an acid concentrating zone. The reaction or absorption zone is divided into two stages, with hydrocarbons flowing through the first and second stages in sequence and sulfuric acid passed into the second stage and forming an extract therein, the extract taken from the second stage and enriched in the first stage and the enrichedextract from the first stage washed with naphthene hydrocarbon or a naphthene base oil and then sent through acid regeneration and acid concentration zones. The hydrocarbon stream passes through first stage reactor 9 and then through second stage reactor I I.

Regenerated acid is fed into second stage reactor I I and forms an extract therein and this extract is fed to first stage 9 to serve as the absorption liquid therein. The enriched extract passes from reactor 9 to settling vessel I and is taken from settling vessel I0 through mixer I3, settling vessel I4, vent drum I5, regenerator I6 and acid concentrator I1 where the acid is restored to its original condition and returned to second stage reactor vessel II. The vent drum I5 is arranged between settling vessel I0 and regenerator tower I6 in order to allow the release of pressure from the extract before it is sent to the regenerator tower. I

In order to eliminate foaming of the acid in vent drum I5, regenerator I 6 and acid concentrator II, the extract is washed to remove foaming agents therefrom. The extract is washed with naphthene hydrocarbon or a naphthene base oil which is added to the extract by a line I9, mixes therewith in mixing device I 3 and subsequently removed from the extract by settling in settling vessel l4. The naphthene hydrocarbon separated from the extract in settling vessel I 4 may be recirculated through line I9 and used for treating additional extract. It will be understood that the naphthene hydrocarbon or naphthene base oil removes foaming agents from the extract and in order to maintain the efiiciency of the naphthene hydrocarbon or naphthene base oil, it is desirable to remove used naphthene hydrocarbon from the system and add fresh naphthene thereto. The used naphthene hydrocarbon may be removed by outlet I9A and fresh naphthene hydrocarbon may be added via inlet I9B to the stream of naphthene hydrocarbon being circulated through line I9.

When the naphthene hydrocarbon or naphthene base oil is added to the sulfuric acid extract and allowed to settle, three layers are formed. The heavier layer is the Washed acid extract which may be withdrawn for the recovery of hydrocarbons therefrom and regeneration of the acid. The middle layer comprises naphthene hydrocarbon admixed with carbonaceous material and the top layer comprises naphthene hydrocarbon substantially free from carbon. In the drawing, the two top'layers may be withdrawn from the settling vessel via line I 9 and recycled.

As a typical example, the hydrocarbon feed stock in vessel I8 may consist of 50% 0; iso and normal butane, 32% normal butylenes and 18% isobutylene. This hydrocarbon mixture is passed from vessel I8 via line 20 in which is arranged pump 2I and heat exchanger 22 and discharges through distributing lines 23 and 24 into first stage reactor vessel 9. The liquid from the bottom of reactor vessel 9 is withdrawn through line 25 and the stream split, with a portion passing through line 26 to first stage settling drum I0 and the remainder being recycled to line 20 via-line To the extract flowing through line 21 is added extract Withdrawn from the second stage settling drum I2 by line 28 and the resultant mixture is discharged into the hydrocarbon stream in line 20.

It is convenient to operate first stage reactor vessel 9 at a temperature of 100 F. and at a pressure of 140 pounds per square inch. Th admixture of the extract comprising sulfuric acid with the hydrocarbon feed stock in line 20 usually results in such a rise in temperature that it is necessary to cool the mixture with heat exchanger '22 in order to maintain the temperature in reactor vessel 9 at approximately 100 F. The hydrocarbon vapors in first stage reactor vessel 9 which are not absorbed or reacted with the sulfuric acid extract therein are removed as overhead via line 29 and discharged into the upper portion of first stage settling drum I0. The unabsorbed hydrocarbons from first stage settling drum ID are passed through line 30 containing heat exchanger 3| and through

lines

32 and 33 into second stage reactor vessel I I. Extract from the lower portion of second stage reactor vessel II is withdrawn via line 34 and the stream split, with a portion passing through line 35 to second stage settling drum I2 and the remainder passing through pump 36 and discharging into the hydrocarbon stream passing through line 30. Regenerated sulfuric acid is discharged into stream 34 through line 31.

Unabsorbed and unreacted hydrocarbon vapors from second stage reactor vessel II pass through line 38 to second stage settling vessel I2 and the unreacted and unabsorbed hydrocarbons from vessel I2 comprising principally iso and normal butane and normal butylenes are withdrawn from outlet line 39. It is convenient to operate second stage reactor vessel I I at a temperature of 70 F. and under a pressure of pounds per square inch and in order to maintain these temperature and pressure conditions in vessel II it will usually be necessary to employ a cooling medium in heat exchanger 3| in order to remove heat resulting from the mixing of hydrocarbons with sulfuric acid in line 30.

With a pressure in first stage reactor vessel 9 of approximately pounds per square inch and in second stage reactor vessel II at approximately 135 pounds per square inch the pressure in first stage settling drum III is approximately 135 pounds per square inch. In order to recover hy-' drocarbons from the extract in settling vessel I0 and regenerate the sulfuric acid used as the extracting agent, it is desirable to release the pressure on the extract and subsequently subject the extract to a heating operation. In order to eliminate foaming in the portion of the system employed for the recovery of hydrocarbons and regeneration of the sulfuric acid, the sulfuric acid extract is washed with a naphthene hydrocarbon or a naphthene base oil before reducing the pressure thereon.

In the drawing, the extract from vessel I0 is withdrawn through line 40 and naphthene hydrocarbon added thereto by line I9 and an intimate mixture of the extract and naphthene hydrocarbon is obtained by passing these components through mixing device I3. The mixture passes from mixing device l3 through line I to settling vessel It. In vessel 14, the upper two layers containing naphthene hydrocarbon maybe withdrawn via line I9 as previously described while the sulfuric acid extract is withdrawnthrough line 40. The sulfuric acid extract passes through line M to vent drum 15 where the pressure on the extract is released to atmospheric by line 4|.

Extract is-withdrawn from vent drum l via line 42 and pump 43 and discharged into regenerator tower l6. Hydrocarbons in vaporous condition are removed from tower it as overhead via outlet 45' and passed into scrubber flfi where they'are brought into contact with caustic introduced into the scrubber through inlet 41. vapors from scrubber 46 are removed through outlet 48 and passed through cooler 09 to condense the high boiling constituents and the portion passing through line 55 and again divided with one part discharged through line 56 into an upper part of regenerator tower I6 and the remainder passing through line 51 containing heater 58 and into regenerator 16 some distance below the point of discharge of line 56. Liquid is withdrawn from the'bottom of scrubber 46 through line 59 and has added thereto condensate withdrawn from vessel 50" via line 52, pump 53 and branch line 60. The liquid mixture in line 59 includes alcohol and polymer and is withdrawn from the system to a suitable arrangement for recovering these valuable products.

It is desirable to operate regenerator tower IS with a bottom temperature of approximately 240 F. and a top temperature of 160 F. In addition to the heat added to the tower by heat exchanger 58, steam may be injected into the bottom of the tower through inlet 6!.

Acid is withdrawn from the bottom of the regenerator tower H5 at a concentration of approximately45% and is passed via line 44 to acid concentrator I1. In this vessel the acid is heated by steam passing throughcoil 62 and the water vapor driven from the acid is discharged through outlet 53. In concentrator vessel ll the acid is concentrated to a strength of approximately 65% and is discharged through line 60 to vessel 65 containing cooling'coil 65 and vent 61. The acid Example I Sulfuric acid of 65% concentration which had been employed in the extraction process for the 10 concentration of isobutylene was tested for its The 29 of sample.

foaming characteristics. Upon passing a stream of air at a rate of 0.038 cubic feet per minute through a 100 cc. sample of the acid it was found that the height of the resulting foam was 37 mm./minute. After the flow of air through the sample was terminated, 10.5 seconds was required for the foam to break.

A sample of the sulfuric acid above tested was washed with a lubricating oil distillate of about 200 seconds Saybolt viscosity at 100 F. obtained from Gulf Coast crude oil in the amount of 3.3 volume per cent of distillate based on the acid. The washed sulfuric acid was blown with air at the rate of 0.038 cubic feet per minute per 100 cc. The height of the foam on the washed sample was 6 mm. and the time required for the foam to break after the flow of air was terminated was 0.6 second.

-A' sample of the unwashed sulfuric acid described in Example I was washed with 3.3 vol.

per cent of a lubricating oil distillate of about 200 secs. Saybolt viscosity at 100 F. which had been obtained by distillation of a Gulf Coast crude-oil and which had been washed and separated from 2 B. sodium hydroxide solution. The

sulfuric; acid which had been washed with the caustic .treated lubricating oil distillate was blown with air at the rate of. 0.040 cu. ft. per min. per 100 cc. of washed acid. The height of the foam on the washed'sample was 8 mm. and the time required for the foam to break after the flow of air was terminated was 1.0 sec.

It is to be understood that the above examples are given by way of illustration and not by way of limitation of the present invention. Wile 3.3 volume per cent of'crude naphthenic acid mixture wa used in the above examples, it will be found that good results may be obtained when naphthene hydrocarbon or a naphthene base oil what I desire to claim is:

' accumulated in vessel is regenerated acid'and is passed through lines 31 and 34 to the hydrocarbon stream passing through line 30 to second stage reactor vessel H. In order to replace the acid lost in the operation, makeup acid may be introduced through inlet line 68 to the stream of regenerated acid.

' When operating the reactor vessels 9 and II at is used in the range of 1 to 20 volume per cent of naphthene hydrocarbon or naphthene base oil for washing the sulfuric acid extract.

Having fully described the present invention 1. A process for separating olefins from a predominately C4 hydrocarbon feed stock comprising olefins including the steps of contacting the feed stock with sulfuric acid in a reaction zone under conditions to form an extract, washing said extra t with a naphthene hydrocarbon oil in a w hing zone under conditions to remove foaming ag nts therefrom, said naphthene hydrocarbon oil being substantially free from naphthenic 05 acids, subsequently heatin the washed extract and reducing the pressure therein to cause the vaporization of a major portion of the hydrocarbons from said extract.

2. A process in accordance with claim 1 in 70 which-the extract is washed with naphthene hydrocarbon oil in the range of 1 to 20 volume per ce minute from vessel l8 and passing 1360 gallon which the sulfuric acid extract is: washed with a; approximately 3 volume per centof a mixture of regenerated acid per minute throughline 3. A process .in accordance with claim 1 in of naphthene hydrocarbons obtained from petro- V 1 of olefins comprising the steps of contacting the hydrocarbon stream with sulfuric acid of a strength of approximately 65 per cent in a reaction zone under conditions to form an extract, removing the extract from the reaction zone and washing it with naphthene hydrocarbon oil in the range of 1 to 20 volume per cent to remove foam-forming agents from the extract, said naphthene hydrocarbon oil being substantially free from naphthenic acids, increasing the temperature and reducing the pressure of the washed extract to cause vaporization of a major portion of the hydrocarbons therein and to form a dilute acid fraction, heating said dilute acid fraction to remove water vapors therefrom and concentrate the acid to-a concentration of approximately 65 per cent and recycling the concentrated acid to 8 the reaction zone and contacting it with said hydrocarbon stream.

5. A method in accordance with claim 4 in which the sulfuric acid extract is washed with approximately 3 volume per cent of a naphthene hydrocarbon oil obtained from petroleum.

JOHN H. CONE.

REFERENCE S CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS