PH26751A - Alkylation catalyst isolation - Google Patents

Description

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ALKYLATION CATALYST ISOLATION

} This invention relates generally to method and apparatus for handling fluids. In one aspect it relates to apparatus for fluid handling in an alkylation process. Ia another aspect it relates to a method for reducing spillage of acidic material in the event of a leak in an alkylation process.

Background of the Invention

It is common practice in the petroleum industry to produce high octane motor fuel by alkylating an isoparaffin with an olefin in the presence of a catalyst which preferably is liquid hydrofluoric acid or hydrogen fluoride (HF). Such a process is commonly known as an HF alkylation process or merely an alkylation process. The effluent from the alkylation reactor containing hydrocarbon and acid, is usually passed to a generally vertical arranged settler vessel at an intermediate point along the length of the settler vessel. A hydrocarbon phase is separated from an acid phase in the settler vessel, with the hydrocarbon phase contained in the upper portion of the settler vessel and the acid phase contained in a lower portion of the settler vessel. Accordingly, a liquid-liquid interface between the acid phase and hydrocarbon phase is formed within the settler vessel. As used herein, the liquid-liquid interface is located at a point along the height of the settler vessel where the acid concentration of the material in the settler vessel is greater by a predetermined amount than the acid concentration in the alkylate product supplied to the settler from the reactor. The hydrocarbon phase is fractionated to separate low boiling hydrocarbons from the alkylate product while the acid phase is cooled and recycled to

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Co : the alkylation reactor for reuse in the alkylation process. As necessary, acid catalyst can be withdrawn from the system for purification. The purified acid catalyst and, as necessary, additional fresh acid is returned to the alkylation reactor.

It is known to improve the economics of an alkylation process by employing two or more alkylation reactors and passing the individual alkylate product streams to a common settler vessel, thereby forming a common pool of acid catalyst in the lower portion of the common settler vessel. Acid catalyst is then withdrawn from the common pool and passed in individual streams to the respective alkylation reactors. While an alkylation system employing multiple reactors and a common acid catalyst pool is effective for reducing equipment cost while maintaining a desired hydrocarbon/catalyst ratio for each reactor, and is also effective for increasing production of high quality gasoline boiling range materials, the system presents certain safety considerations. For example, with a common acid catalyst pool, a leak in one reactor could result in spillage of the entire catalyst pool which supplies the multiple reactors.

Acid catalyst fluid handling systems associated with alkylation processes are designed with due concern for providing a non-leaking catalyst fluid handling system. In order to provide greater safety, however, it is desirable to reduce, as much as possible, the spillage that would occur in the event of a leak affecting the liquid acid catalyst.

Accordingly, it is an object of this invention to improve safety in operating an alkylation process.

A further object of this invention is to increase the safety of a petroleum refining process and the apparatus employed therein.

Another object of this invention is to provide apparatus and method for reducing the spillage of acid catalyst in the invent of a leak in the acid catalyst handling system associated with an alkylation process.

Summary of the Invention

In accordance with one aspect of this invention, multiple chambers are provided in the bottom of a common acid settler vessel to contain the acid catalyst. The number of chambers provided at least corresponds to the ocumber of respective reactors which supply alkylate product to the common settler vessel. Separate acid return streams for each reactor are also provided so that a leak in one reactor, or its associated acid cooler, would result in liquid spillage of po more than the amount of the acid catalyst io the chamber of the common settler vessel associated with that reactor.

In accordance with another aspect of this invention the common settler vessel is operated with both liquid and gaseous hydrocarbon phases at lower pressures, 30 that the leak rate resulting from a leak in a reactor would be minimized.

In a preferred embodiment of this invention a comaon settler vessel is provided with at least one baffle extending from wall to wall at the bottom of the common settler vessel and upwardly into close proximity, or above, the interface between the liquid acid catalyst phase and the liquid hydrocarbon phase in the common settler vessel.

The baffle separates the lower portion of the settler vessel into two or more chambers and prevents liquid communication between the quantities of liquid acid catalyst which are contained within the chambers and are to be recycled to the respective reactors. A separate outlet is provided for each chamber in the bottom of the common settler vessel for return of the acid catalyst to the respective reactor and associated cooler.

Should the acid catalyst level lower in ome chamber due to ' leakage or spillage, liquid hydrocarbon from the correspondingly lowered hydrocarbon phase thereabove displaces the acid catalyst volume lost and thus provides 3 liquid seal for the acid catalyst ia the noan-leaking chambers. Also, another paterial which is less dense and of higher boiling point than the acid catalyst, could be injected to replace the . spilled acid catalyst and provide the liquid seal.

In a preferred embodiment of the present invention, four reactors, each having aa associated cooler, are utilized. Two riser reactors are positioned oo two opposite sides of a vertically oriented settler vessel. Alkylate product streams of the two reactors oa one side of the settler are combined at or above the elevation of the settler inlet, and enter the settler in 3 combined stream. In a similar manoer the alkylate product of the two reactors on the other side of the settler fier Nop erie, 07 THE LeAwiné > 32405US . 4 / vessel are combined and enter the settler vessel in a single stream. / Four separate streams are provided for returning the acid catalyst from - the settler to four corresponding riser reactors via four corresponding acid catalyst coolers. —""" f4ditional objects and advantages of the invention will be apparent from the following detailed description of the preferred embodiment of the invention as illustrated by the drawings in which:

FIG. 1 is a diagrammatic elevation of riser reactors, a settler vessel and coolers provided ian an arrangement suitable for carrying out the invention.

FIG. 2 is a side elevation taken along line 2-2 of FIG. 1.

FIG. 3 is a side elevation taken along lines 3-3 of FIG. 1.

FIG. 4 is a cross sectional view taken along line 64-4 of

FIG. 1.

Detailed Description of the Preferred Embodiment

In the following discussion, parts which appear in more than one of the drawing figures shall be referred to by the same reference numeral in each of the drawing figures in which the part appears.

Referring now to the drawings and in particular to FIGS. 1, 2 and 3, four upwardly extending tubular reactors, referred to hereinafter as riser reactors, are designated by the reference characters 10, 11, 12 and 13 and are in open communication at the tops thereof with a generally vertically disposed settler vessel 14 via conduits 16, 17, 18 and 19.

The settler vessel 14 defines a vertically extending separation zone therewithin having a lower portion, an upper portion and an intermediate portion. The settler vessel 14 provides means for separating a mixture containing a heavier liquid and a lighter liquid. Effluent alkylate, together with acid catalyst, is introduced into a lower portion of the settler 14 from the outlets of reactors 10, 11, 12 and 13 through conduits 16, 17, 18 and 19. Although four reactors are illustrated in FIGS. 1-4, any oumber of reactors can be used in the practice of the invention.

The lower ends of riser reactors 10, 11, 12 and 13 are in open fluid communication with coolers 20, 21, 22 and 23, respectively.

Hydrocarbon feed is provided via conduit 24 to coolers 20, 21, 22 and 23 along with additional fresh acid where cooled recycled or rerun acid

Ce — catalyst is picked up to form a hydrocarbon and acid catalyst mixture.

The hydrocarbon and acid catalyst mixture is dispersed upwardly with high velocity through the coolers 20, 21, 22 and 23 and into the corresponding inlets of riser reactors 10, 11, 12 and 13, respectively. 5 At the bottom of common settler vessel 14, outlet conduits 26, 27, 28 and 29, which extend downwardly from settler vessel 14, are provided for the withdrawal of liquid acid catalyst for recycle.

Conduits 26, 27, 28 and 29 are connected at the lower ends thereof with coolers 20, 21, 22 and 23, respectively via corresponding coaduits 30, 31, 32 and 3). At an intermediate point aloog the length of the settler vessel 14 aan outlet conduit 34 is provided for the removal of the separated liquid hydrocarbon product. 1n operation, 3 liquid hydrocarbon feed mixture comprising 2 mixture of ano alkylating agent, such as a lov boiling olefin, e.g. butylene, and an alkylatable hydrocarbon, such as a low boiling isoparaffio, €.8- isobutane, is introduced through conduit 24, as well as fresh makeup acid catalyst. The feed mixture is dispersed at high velocity in the shells of coolers 20, 21, 22 and 23 which contain cooled liquid acid catalyst, thus inducing acid catalyst circulation into the hydrocarbon feed mixture by density difference between the settled acid 38 from the settler 14 and the fresh makeup acid catalyst dispersed with the hydrocarbon feed. In this manner acid catalyst is picked up by the flow action of the liquid hydrocarbon feed mixture. Hydrocarbon feed mixture and cooled recycled acid catalyst pass through the reactors 10, 11, 12 and 13 in co-current flow which results in formation of higher molecular weight hydrocarbon material or alkylate of increased octane value, as is well known in the art.

Reaction effluent, containing alkylate (i.e. hydrocarbon product), catalyst aod unreacted feéd hydrocarbon, passes from reactors - 30 10, 11, 12 and 13 and enters settler vessel 14 through conduit 16, 17 18 and 19. Within settler vessel 14, the effluent from reactors 10, 11, 12 and 13) separates into 2 lower liquid acid phase and ao upper liquid hydrocarbon phase. Ino accordance with the invention, however, settler vessel 14 is preferably operated with both liquid and gaseous hydrocarbon phases, 33 illustrated in FIG. 1.

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A liquid-liquid interface is formed at a point 36 in settler vessel 14. The iatecface occurs at the level between the lower heavy acid phase 38 and the lighter hydrocarbon phase 40. As used berein the interface 36 is considered to be the point along the vertical length of

S the chamber of the common settler vessel 14 where the acid concentration of the material settled in the lower portion of settler vessel 14 is equal to, or greater by a predetermined amount, than the acid concentration io the reactor effluent material supplied to the common settler vessel 14, through conduits 17 and 19.

As most clearly illustrated in FIG. &, the lower portion of common settler vessel 14 is provided with baffles 50 and 52 which divide the lower portion of vessel 14 into four chapbers 54, 56, 58, and 60.

As illustrated most clearly in FIGS. 1, 2 snd 3, the baffles 50 and 52 extend from the bottom of the settler vessel 14, at least iato close proximity to the interface level 36. Thus, acid catalyst supplied to settler vessel 14 from 2 pair of riser reactors on ome side of the settler vessel 14, and which descends mostly along the walls of settler vessel 14, is for the most part returned to the respective pair of riser ‘reactors.

An alkylatioa unit euch as shown in the drawings may be operated such that the interface level 36 is different in the various chambers S54, 56, 58 and 60. The baffles 50 and 52 therefore may extend upwardly to near proximity of the interface level in one chamber while extending significaatly above the interface level in an adjacent chamber. 26 Accordingly, the baffles 50 and 52 may be any desired height and may extend significantly into the hydrocarbon settling zone 40 if desired.

The requirement for the baffles 50 and 52 is that they extend to a height sufficient to assure that the chambers 54, 56, S8 and 60 coatain substantially all of the acid catalyst in the lower portion of settler

Co 30 vessel 14. " The acid catalyst is withdrawn from the chambers 54, 56, s8 and 60 through outlets 62, 64, 66 and 68, respectively, {llustrated in

FIG. &4, which outlets are provided in the bottom of common settler vessel 14 and are connected in fluid flow comuunication with conduits 28, 26,

_ Ce —— — - — —_—— 32405US 7 27 and 29, respectively, and the acid catalyst is recycled to the riser reactors via the coolers and interconnecting conduits.

The invention is not dependent upon specific reaction conditions, or reactants, as these are conventional and well known in the art. It is, however, as previously stated, desired to operate the common settler 14 less than liquid full and at a low pressure, so as to minimize the leakage rate in the event of a failure.

For reasons of brevity, conventional auxiliary equipment such as pumps, additional feed lines, additional heat exchangers, measurement and control devices, etc. have not been included in the above description as they play no part in the explanation of the invention.

The invention is thus broadly applicable to containing heavy liquid in a settler vessel. Various modifications of this invention, such as providing additional chambers for the containment of the acid catalyst, can be made in view of the foregoing disclosure and the appended claims. Such variations and modifications are within the scope of the present inventiou as claimed.

Claims (1)

1. We claim:

   1. Apparatus comprising: a vessel defining a separation zone having a lower portion, an intermediate portion and an upper portion for separating a mixture containing a heavier liquid and a lighter liquid; means for introducing said mixture containing a heavier liquid and a lighter liquid into said separation zone, to form a liquid-liquid interface in said separation zone, said interface occurring at a level between said heavier liquid and said lighter liquid, and wherein said heavier liquid is contained in said lower portion of said separation zone and wherein said means for introducing a mixture comprises reactor means for alkylating olefins with isoparaffins in the presence of a hydrogen fluoride catalyst; means for passing reactor effluent comprising liquid hydrogen fluoride catalyst and liquid hydrocarbon product from said reactor means into said separation zone; and means disposed within said vessel for dividing said lower portion of said separation zone into a plurality of chambers, for containing at least a major portion of said heavier liquid so that any leak resulting in the draining of said heavier liquid from any individual chamber of said plurality of chambers will not correspondingly result in the draining of said heavier liquid from the remaining unaffected chambers of said plurality of chambers.

   2. Apparatus in accordance with claim 1, wherein said means for dividing comprises: a baffle extending upwardly from the bottom of said lower portion of said separation zone to a location proximate said interface.

   3. Apparatus in accordance with claim 1, wherein said means for dividing comprises: a baffle extending upwardly from the bottom of said lower portion of said separation zone into said intermediate portion of said separation zone. 4, Apparatus comprising: a vessel defining a separation zone having a lower portion, an intermediate portion and an upper portion for separating a mixture containing a heavier 1liaguid and a lighter 1iaguid:

   liquid hydrocarbon ‘product to separate in said separation zone whereby a liguid-liquid interface is formed in said separation zone at the level between said liquid acid catalyst and said liquid hydrocarbon product, and wherein a major portion of said liquid acid catalyst is contained in said plurality of chambers in said lower portion of said separation zane.

   11. In an alkylation process wherein the amount of liquid acid catalyst required to maintain a desired liquid acid catalyst required to maintain a desired liquid acid catalyst/liquid hydrocarbon product ratio in a plurality of alkylation reactors is contained in the lower portion of a common settler vessel operatively connected to said plurality of alkylation reactors, the improvement comprising: dividing the lower portion of said common settler vessel into a plurality of chambers for containing a desired amount of liquid acid catalyst so that a leak resulting in the draining of liquid acid catalyst from one -of the plurality of alkylation reactors will spill no more than the amount of liquid acid catalyst contained in one of said plurality of chambers and will not affect the liquid acid catalyst level in any of the other of said plurality of chambers.

   12. A method in accordance with claim 10, comprising the additional step of: operating said common settler vessel less than liquid full so as to form a gaseous hydrocarbon phase in said upper portion of said separation zone.