Ionic liquid reactor with heat exchanger

An ionic liquid reactor unit and a process for controlling heat generation from an ionic liquid reactor unit. The ionic liquid reactor unit may include an external heat exchanger. The effluent from the reactor is separated in a separation zone allowing the hydrocarbon phase to transfer heat to a cooling fluid. The heat exchanger may be a tube-in-shell, a spiral plate heat exchanger, a hair pin heat exchanger. The heat exchanger accommodates the separation of the ionic liquid from the hydrocarbon phase, and may allow for the ion liquid to be drained.

FIELD OF THE INVENTION

This invention relates generally to an ionic liquid reactor and more particularly to an ionic liquid reactor with a heat exchanger.

BACKGROUND OF THE INVENTION

Ionic liquids are essentially salts in a liquid state, and are described in U.S. Pat. No. 4,764,440, U.S. Pat. No. 5,104,840, and U.S. Pat. No. 5,824,832. The properties vary extensively for different ionic liquids, and the use of ionic liquids depends on the properties of a given ionic liquid. Depending on the organic cation of the ionic liquid and the anion, the ionic liquid can have very different properties. The behavior of the ionic liquid varies considerably for different temperature ranges, and it is preferred to find ionic liquids that do not require operation under more extreme conditions such as refrigeration.

Acidic ionic liquid may be used as a catalyst in various chemical reactions, such as for the alkylation of iso-butane with olefins. The alkylation reaction is highly exothermic. To control the temperature, it is common for part of the unreacted light hydrocarbons to be vaporized. However, controlling the temperature by vaporization is undesirable because it makes the reactor operation, the ionic liquid dispersion, and the acid concentration more difficult to control. Therefore, it is believed to be more desirable to control the temperature while the reactants and products are maintained in liquid form.

While it would be desirable to utilize heat exchange to control the temperature, any heat exchanger will need to be configured to minimize the impact of the ionic liquid phase on heat transfer due to its high viscosity and potential for fouling of the heat transfer surface.

Additionally, as will be appreciated, conjunct polymer is often a byproduct of the various ionic liquid catalyst reactions including but not limited to alkylation, oligomerization, isomerization, and disproportionation. Conjunct polymer is typically highly conjugated, olefinic, highly cyclic hydrocarbons. The conjunct polymer is often associated with ionic liquid and will also impact heat transfer in similar ways as ionic liquid.

It would be desirable to provide an ionic liquid reactor that can effectively control the heat produced by exothermic reactions without the need of vaporization. It would also be desirable for such a reactor to account for the presence of conjunct polymer and ionic liquid catalyst.

SUMMARY OF THE INVENTION

An ionic liquid catalyst reactor and a process for controlling the heat of an ionic liquid catalyst reaction have been invented. The ionic liquid catalyst reactor and process utilize at least one external heat exchanger to remove the heat produced by the exothermic reactions. The various heat exchangers are designed to accommodate the hydrocarbons as well as the ionic liquid catalyst and the conjunct polymer that have a tendency to foul the equipment.

In a first aspect of the present invention, the invention may be broadly characterized as providing an ionic liquid catalyst reactor unit comprising: a first reaction zone having an inlet for ionic liquid, an inlet for a hydrocarbon stream, and an outlet for an effluent stream; a separation zone configured to receive the effluent stream and separate the effluent stream into a hydrocarbon phase and an ionic liquid phase; and, a first heat exchange zone configured to receive at least a portion of the effluent stream from the first reaction zone. The first heat exchange zone comprises an outlet for a cooled effluent stream, and an outlet for ionic liquid.

In various embodiments of the present invention, the first heat exchange zone comprises a heat exchanger with a shell and wherein the separation zone is disposed within the shell. It is contemplated that the shell includes an inlet for the effluent stream disposed below the outlet for the cooled effluent stream.

In some embodiments of the present invention, the first heat exchange zone comprises a heat exchanger comprising a shell and at least one baffle in the shell. It is contemplated that the at least one baffle comprises a baffle selected from the group consisting of: a helical baffle; a rod baffle; a grid baffle; an expanded metal baffle; and, a segmental baffle. It is also contemplated that the heat exchanger is configured to receive the effluent stream in a direction countercurrent to a direction of cooling fluid through the heat exchanger.

In various embodiments of the present invention, the first heat exchange zone comprises a spiral plate heat exchanger having a first flow path configured to receive the effluent stream and a second flow path configured to receive a cooling fluid. It is contemplated that the spiral plate heat exchanger comprises a collection pan and at least one flow path includes one or more openings to allow ionic liquid to drain from the at least one flow path to the collection pan.

In one or more embodiments of the present invention, the first heat exchange zone comprises at least one hair pin heat exchanger. It is contemplated that the at least one hair pin heat exchanger includes a boot configured to allow ionic liquid to be drained from the at least one hair pin heat exchanger.

In some embodiments of the present invention, the first heat exchange zone comprises at least one tube-in-shell heat exchanger having a horizontal orientation and comprising tubes inside of a shell with an inlet for an effluent stream on a top of the shell, and an outlet for a cooled effluent stream on a bottom of the shell. It is contemplated that the shell further comprises a boot configured to allow ionic liquid to be drained from the at least one tube-in-shell heat exchanger. It is further contemplated that the at least one tube-in-shell heat exchanger further comprises at least one grid baffle disposed within the shell.

In many embodiments of the present invention, the ionic liquid catalyst reactor unit further comprises: a second reaction zone having an inlet for ionic liquid, an inlet for a hydrocarbon stream, and an outlet for an effluent stream; and, a second heat exchange zone configured to receive at least a portion of the effluent stream from the second reaction zone and comprising an outlet for a cooled effluent stream and an outlet for ionic liquid. The first heat exchange zone may be disposed between the first reaction zone and the second reaction.

In at least one embodiment of the present invention, the ionic liquid catalyst reactor unit further comprises a plurality of reaction zone each having an inlet for ionic liquid, an inlet for a hydrocarbon stream, and an outlet for an effluent stream, the reaction zones arranged in series and, a plurality of heat exchange zones. It is preferred that at least one heat exchange zone is disposed between successive reaction zones.

In a second aspect of the present invention, the invention may be broadly characterized as providing process for controlling the temperature of a reaction performed in the presence of an ionic liquid catalyst by: performing a reaction in the presence of an ionic liquid catalyst to form an effluent, wherein the reaction is performed in a reaction zone; removing heat from at least a portion of the effluent from the reaction zone in a heat exchange zone with a cooling fluid to provide a cooled effluent; and, separating the effluent in a separation zone into a hydrocarbon phase and an ionic liquid phase.

In some embodiments of the present invention, the process include separating ionic liquid from the effluent from the reaction zone within the heat exchange zone. It is contemplated that the process includes passing the ionic liquid separated from the effluent in the heat exchange zone to a second reaction zone. It is further contemplated that the process also includes performing a reaction in the presence of an ionic liquid catalyst to form a second effluent, wherein the reaction is performed in the second reaction zone, and, passing the second effluent from the second reaction zone to a second heat exchange zone. It is also contemplated that the process further includes separating ionic liquid from the second effluent in the second heat exchange zone, and removing heat from the second effluent from the second reaction zone in the second heat exchange zone with a cooling fluid to provide a second cooled effluent.

Additional aspects, embodiments, and details of the invention, which may be combined in any manner, are set forth in the following detailed description of the invention.

DETAILED DESCRIPTION OF THE INVENTION

As mentioned above, an ionic liquid catalyst reactor and a process for controlling the heat of an ionic liquid catalyst reaction have been invented which utilize an external heat exchanger. The heat exchanger is designed to allow reactants and ionic liquid acid catalyst to be in liquid phase. A heat exchange fluid will absorb heat from the reactor effluent mixture. By controlling the temperature with the heat exchanger and, more importantly without vaporization of the reactants, products, or ionic liquid, it will be easier to control the reactor operation, ionic liquid dispersion and acid concentration.

With these general principles of the present invention in mind, one or more exemplary embodiments of the present invention will now be described with the understanding that the following is exemplary in nature and is not intended to be limiting.

As shown inFIG. 1, a reactor unit10according to various embodiments of the present invention comprises at least one reaction zone11aand at least one heat exchanger14a. In addition to the at least one reaction zone11aand the at least one heat exchanger14a, the reactor unit10may further comprise at least one separation vessel16a.

In a preferred embodiment, a plurality of reaction zones11a,11b,11c,11d,11eare provided. For example, each of the reaction zones11a,11b,11c,11d,11emay comprise a reactor vessel12a,12b,12c,12d,12e, with the reactor vessels12a,12b,12c,12d,12ebeing arranged in series. It should be appreciated that although not depicted as such, a single reactor vessel could be used with multiple separate reaction zones11a,11b,11c,11d,11econtained within the single vessel. The at least one heat exchanger14ais disposed between the reaction zone11aand the at least one separation vessel16a. Preferably, one heat exchanger14a,14b,14c,14dfrom a plurality of heat exchangers14a,14b,14c,14dis disposed between successive reaction zones11a,11b,11c,11d,11e, as shown inFIG. 1.

In a preferred embodiment, the reactor unit10is utilized for an alkylation reaction, and therefore the present invention will be described in relation to an alkylation reaction, with the understanding that the present invention is not necessarily limited to same and can be practiced in association with different exothermic reactions.

As shown inFIG. 1, an iC4hydrocarbon stream18comprising iC4hydrocarbons is passed into the first reactor vessel12a. An olefin hydrocarbon stream20comprising C4olefinic hydrocarbons is also passed into the first reactor vessel12a. The olefinic hydrocarbon stream20can include iC4hydrocarbons as well to dilute the olefinic hydrocarbons before entering the reactor vessel12a. The overall concentration of iC4hydrocarbons in the reactor vessel12ais preferably well above the stoichiometric requirement of the alkylation reaction to minimize the side reactions of olefins with non-iC4hydrocarbons.

An ionic liquid catalyst stream22is also passed into the first reactor vessel12a. As shown, the ionic liquid catalyst stream22is mixed with the iC4hydrocarbon stream18prior to being passed to the first reactor vessel12a. This is merely preferred.

In the first reactor vessel12a, which is operated under proper conditions, such as at a temperature of between 4.4° to 37.8° C. (40° to 100° F.) under a pressure that keeps all reactants and catalysts in liquid phase, the olefinic hydrocarbons will react with the iC4hydrocarbons to form alkylated hydrocarbons, primarily iso-octane and other trimethylpentanes. In order to mix the ionic liquid catalyst and the hydrocarbons, the first reactor vessel12aincludes an impeller24a. The impeller24amay also disperse the ionic liquid catalyst. The products of the reaction, as well as excess reactants (mainly iC4hydrocarbons) and the ionic liquid catalyst are passed out of the first reactor vessel12ain an effluent stream26a.

The effluent stream26afrom the first reactor vessel12ais passed to the first heat exchanger14a. As shown inFIG. 1, the heat exchanger14acomprises a shell28awith multiple U-shaped tubes30awithin the shell28a. The U-shaped tubes30acontain a heat exchange fluid, such as water or a refrigerant. As shown, the heat exchanger14ainFIG. 1has a vertical orientation (i.e., a longitudinal axis of the heat exchanger14ais generally vertical).

The effluent stream26afrom the first reactor vessel12ais preferably passed into the heat exchanger14ainto a lower or bottom portion that comprises a separation zone32a. The separation zone32aallows the heavier ionic liquid catalyst phase to separate from the effluent and accumulate on the bottom (due to the larger specific gravity compared to the hydrocarbons). The remaining components of the effluent will flow upwards in the shell28aand contact the U-shaped tubes30awith cooling fluid flowing through the tube side.

As will be appreciated, the cooling fluid in the U-shaped tubes30awill absorb heat from the effluent in a heat exchange zone31aof the heat exchanger14a. In this embodiment, the separation zone32aand the heat exchange zone31aare contained within the shell28a, or housing, of the heat exchanger14a. It is also contemplated, but not shown that the separation zone32ais within a separate vessel so as to allow for separation of the ionic liquid phase and the hydrocarbon phase prior to the effluent (or at least a portion thereof) passing into the heat exchange zone31a.

Returning toFIG. 1, the heat exchanger14aalso includes baffles that may support the tubes and/or direct flow to improve heat transfer. A preferred baffle type is a helical baffle34a. Any ionic liquid, or conjunct polymer, which separates from the effluent above the separation zone32amay flow downward along the helical baffle34ato the bottom of the heat exchanger14a. In addition, the helical baffle34aalso streamlines the flow of fluid and reduces the creation of any stagnant zones in the heat exchanger14aat the baffle (which would create accumulation of materials and restrict flow and heat exchange). Thus, while as would be appreciated other baffle types may be considered, the preferred helical baffle34aminimizes the fouling tendency of ionic liquid and conjunct polymer passing through heat exchanger14aand the negative impact on heat transfer from same.

A portion of a cooled effluent stream36amay be passed from the heat exchanger14ato the separator vessel16a. A second portion of the cooled effluent stream36amay be passed to the second reactor vessel12b. Additionally, an ionic liquid catalyst stream38afrom bottom of the heat exchanger14amay also be passed to the second reactor vessel12b, passed to the first separation vessel16a, or a combination thereof.

The second reactor vessel12bwill receive iC4hydrocarbons (and other hydrocarbons) from the cooled effluent stream36a, a second olefin hydrocarbon stream20bcomprising C4olefinic hydrocarbons, and a second ionic liquid stream, in this case, from the ionic liquid catalyst stream38afrom bottom of the heat exchanger14a. The second reactor vessel12bmay also receive an ionic liquid stream that comprises ionic liquid that may have separated in the first reactor12a. The second reactor vessel12bpreferably operates in the same manner and under similar conditions as the first reactor vessel12aand, thus will likewise produce an effluent stream26bcontaining more alkylate components than effluent stream26a.

The effluent stream26bfrom the second reactor vessel12bwill be passed to the second heat exchanger14b, which will function similarly to the first heat exchanger14a. A cooled effluent stream36bfrom the second heat exchanger14bmay be passed to a third reactor vessel12c, and so on and so forth. As shown inFIG. 1, at the last reactor vessel, reactor vessel12e, an effluent stream26eis shown as being passed to the first separation vessel16ainstead of a heat exchanger. Such a configuration is preferred because it will lower the cost associated with the reactor unit10by not requiring an additional heat exchanger. Additionally, the increased temperature in the separation vessels16aand16bprovided by the effluent stream26efrom the last reactor will facilitate better separation between the ionic liquid catalyst phase and the hydrocarbon phase. However, it should still be appreciated, that a heat exchanger could be disposed between the last reactor vessel and the first separation vessel16a. As would be appreciated, the numbers of reactor vessels and heat exchangers can be varied for increased operation flexibility and vary from the exemplary embodiment shown inFIG. 1.

In the first separation vessel16a, a mixture comprised of the effluent streams from the reaction zones11a,11b,11c,11d,11eand ionic liquid catalyst streams will separate into a lighter hydrocarbon phase40and a heavier, ionic liquid catalyst phase42. Preferably, in the first separation vessel16a, at least 50%, and more preferably at least 90% of the ionic liquid catalyst will be separated from the hydrocarbons due to the different densities of the phases. The ionic liquid catalyst phase42can be withdrawn in an ionic liquid catalyst stream44, which can be reused in the process, which can be regenerated, which can be disposed of, or a combination thereof. The hydrocarbon phase40can be withdrawn in a hydrocarbon effluent stream46which may be passed to a second separation vessel16b.

In the second separation vessel16b, entrained droplets of ionic liquid catalyst within the hydrocarbon phase40from the first separation vessel16amay be further separated, for example with a coalescer material48, such as glass beads, fibers or electrostatic separation devices. A second ionic liquid catalyst stream50(the numeral “52” near bottom ofFIG. 1should be changed to “50”) comprising ionic liquid catalyst separated in the second separation vessel16bcan be combined with the ionic liquid catalyst stream44. A hydrocarbon product stream52, in this case comprising an alkylate product, can be passed from the second separation vessel16bto a fractionation column (not shown) or other separation unit to separate the various hydrocarbons in the product stream52. In various embodiments, the amount of ionic liquid in the hydrocarbon product stream52is preferably less than 100 ppm, and more preferably less than 20 ppm.

In another heat exchanger100, shown inFIG. 2, the cooling fluid and the reactor effluent, for example the reactor effluent26ashown inFIG. 1, preferably flow at least partially in a countercurrent manner to increase the cooling function of the cooling fluid.

In the embodiment shown, the heat exchanger100comprises a shell102with an inlet106proximate a first end108of the shell102and an outlet110proximate a second end112of the shell102. A plurality of U-shaped tubes114extend from one end of the shell102, preferably the first end108, towards the second end112of the shell102. The U-shaped tubes114will receive cooling fluid, which can pass from a cooling fluid inlet116to an inlet manifold118which will distribute the cooling fluid to the tubes114. The heated cooling fluid may flow to an outlet manifold120and then be withdrawn through an outlet122and used elsewhere if desired. The hydrocarbons and ionic liquid will pass from the inlet106of the shell102to the outlet110of the shell102, with the flow path between the inlet106and the outlet110being partially counter-current to the flow of cooling fluid through the tubes114. Straight tubes extending from the first end108of the shell102to the second end112can also be used in the heat exchanger100. The heat exchanger may include one or more baffles123.

For example, a plurality baffles123may be disposed within the shell102between the inlet106and the outlet110. As shown inFIG. 3, the baffles123may comprise a plurality of rods204arranged to form a grid baffle200with a plurality of openings202for the fluids to flow there through and for the tubes114to extend there through. The rods204may be horizontal, vertical, or angular. As will be appreciated, the rods204need not be extended cylindrical members, but can be strips of material, dimpled sheets, or other shaped members. Additionally, the rods204can be configured in other designs and arrangements, such as alternating horizontal and vertical rods as shown in U.S. Pat. No. 5,139,084. Additionally, instead of rods204, the baffles123may comprise alternating segmental baffles, such as shown in U.S. Pat. No. 4,699,211.

Returning toFIG. 2, the shell102of the heat exchanger100may also include a boot124to allow any ionic liquid that separates out to accumulate and be withdrawn from the heat exchanger100via an outlet126. Multiple boots124or one boot124connecting multiple draining nozzles along the bottom of the heat exchanger100can be used. As shown, the heat exchanger100has a horizontal orientation, but an angular orientation could also be used.

Turning toFIGS. 4 and 5, another heat exchanger is shown which is contemplated to be used for the reactor and processes of the present invention in which the heat exchanger comprises a spiral plate heat exchanger300. The spiral plate heat exchanger300includes a housing302, or shell, and at least one plate channel304inside of the housing302that provides two spiral flow paths306,308. The first flow path308includes an inlet310preferably on a top312of the housing302and an outlet314, preferably on a side surface316of the housing302. The second flow path306includes an inlet318, preferably on the side surface316of the housing302, and an outlet320, preferably on the top312of the housing302. As will be appreciated, the references to “top” and “side” are in relation to the orientation shown in the Figures. Any change in the orientation of the heat exchanger300may result in the “top” being the “side.”

In any orientation, the flow paths306,308are preferably countercurrent in order to maximize the temperature difference between the two streams and increase the heat exchange, and thus the cooling, of the effluent stream. It is preferred that the inlet318for the second flow path306and the outlet314for the first flow path308are disposed 90 degrees apart along the side surface316of the heat exchanger300.

As can be seen inFIG. 5, the heat exchanger300also includes a collection pan322for ionic liquid catalyst that can be used to collect the ionic liquid that separates from the effluent in the heat exchanger300.

More specifically, the ionic liquid will be separated from the hydrocarbons along one of the flow paths306,308containing ionic liquid and hydrocarbons inside the heat exchanger300as a result of the density difference between ionic liquid and the hydrocarbon. Additionally, centrifugal flow through the flow paths306,308will accelerate the ionic liquid separation. In this case a separation zone and a heat exchange zone will both be contained within the housing302of the heat exchanger300.

The settled ionic liquid at the bottom of one of flow paths306,308can be drained into the collection pan322via one or more openings324. In order to minimize the amount of the hydrocarbon phase that may pass through the openings, it is preferred that the openings are sized and disposed such that less than 10% of the total hydrocarbons, and preferably less than 5% of the total hydrocarbons, passes there through. The ionic liquid is preferably drained through a bottom boot326as, for example the ionic liquid catalyst stream38aas shown inFIG. 1. It is also contemplated that the heat exchanger300includes individual drains on one or more revolutions of one of the spiral flow paths306,308where the ionic liquid could be drained. These individual drains can be connected to valves or a boot or a separate vessel for removing ionic liquid.

The ionic liquid withdrawal rate from the separation zones and/or the ionic liquid level in the separation zones such as the bottom of heat exchangers inFIG. 1, the boots inFIG. 2and the pan inFIG. 5can be controlled to minimize the hydrocarbon entrainment in the ionic liquid.

Since some of the more viscous and heavier ionic liquid and conjunct polymer is separated from the reactor effluent before or within the heat exchangers, the heat transfer is improved and pressure drop reduced along the flow path due to less ionic liquid and conjunct polymer being present in the heat exchange zone and contacting the heat exchange surface (i.e., the spiral plate304).

It is contemplated alternatively that the heat exchanger300with the spiral plate304is rotated 90 degrees (about the horizon) so that the flow of fluids is in a vertical direction (as opposed to a horizontal direction). In this case, the ionic liquid will not be separated from hydrocarbon in the spiral plate heat exchanger300and instead can be passed along to a sequential reactor or to a separation vessel or other equipment.

Another possible heat exchange configuration that may be utilized in accordance with the present invention is shown inFIG. 6. InFIG. 6, two hairpin heat exchangers400a,400b, are arranged in series. Although two hairpin heat exchangers400a,400bare shown, any number may be used, for example, one, more than one, two, etc.

With reference to the first hairpin heat exchange400a, the hairpin heat exchange400aincludes a shell402awith an inlet406aand an outlet410a. Extending within the shell402ais at least one tube414aalso having an inlet416aand an outlet422a. As will be appreciated, the hairpin heat exchange400ais designed so that the flow on the tube side is countercurrent to the flow on the shell side. Thus, the inlet406afor the shell402aand the outlet422afor the tube414aare disposed proximate the same end of the hairpin heat exchange400a. If the flow on the tube side and the flow on the shell side was co-current, the inlet422afor the shell402aand the inlet416aon the tube414awould be disposed proximate each other on the same end of the hairpin heat exchange400a. The remaining disclosure will utilize a preferred countercurrent flow, as it maximize the temperature differences between the hot and the cold fluids, with the understanding that a co-current flow could be utilized. Furthermore, in a preferred embodiment, reactor effluent (for example the reactor effluent26a,FIG. 1) flows on the shell side and the cooling fluid flows on the tube side of the hairpin heat exchange400a. Again, this configuration is merely preferred. The heat exchanger400aalso may include one or more baffles423a. The baffles423amay comprise one or more helical baffles, rod baffles, segmental baffles, or any other baffles. Finally, while the heat exchanger400ais shown having a horizontal orientation, it is contemplated that a vertical or an angular orientation could also be used.

In use, the reactor effluent may pass through the inlet406aof the shell402aand flow towards the outlet410aof the shell402a. Ionic liquid may separate from the reactor effluent and can accumulate in one or more boots424adisposed on the shell402a. Any ionic liquid that separates out may be withdrawn from the heat exchanger400avia an outlet426a. Multiple boots424aor one boot424aconnecting multiple draining nozzles along the bottom of the heat exchanger400acan also be used. As shown preferably only the upper longitudinal portion of the heat exchanger400aincludes boots424afor removing ionic liquid. The exact location and number of boots424a, including none, can vary. Cooling fluid may pass through the inlet416aof the tube414aand flow towards the outlet422a. As it passes through the tube414a, it will absorb heat from the reactor effluent.

While only one heat exchanger400amay be used, as shown inFIG. 6a second heat exchanger400bis shown in series. The second heat exchanger400bmay be the same or similar to the first heat exchanger400band thus the same components have similar reference numerals except for the “b” for the components of the second heat exchanger400b. Furthermore, it is contemplated that the second heat exchanger400bnot include any boots. As shown a first conduit460, such as a pipe or hose, connects the outlet410aof the shell402aof the first heat exchanger400ato the inlet406bof the shell402bof the second heat exchanger400b. Similarly, a second conduit462connects the outlet422bof the tube414bof the second heat exchanger400bto the inlet416aof the tube414aof the first heat exchanger400a. Thus, the cooling fluid will flow from the second heat exchanger400bto the first heat exchanger400a, while the reactor effluent will flow from the first heat exchanger400ato the second heat exchanger400b.

It is preferred to remove ionic liquid at locations close to the effluent inlet in the first heat exchanger so that the impact of ionic liquid and the associated conjunct polymer on the heat transfer downstream can be minimized. Additional withdrawal of ionic liquid along the flow path of the reactor effluent is optional.

With any of the various heat exchangers disclosed herein, it is believed that the fouling of the heat exchanger by the ionic liquid and conjunct polymer will be minimized through the separation of ionic liquid from reactor effluent, allowing the heat exchanger to remain effective for controlling the temperature of the reactor effluent.

It should be appreciated and understood by those of ordinary skill in the art that various other components such as valves, pumps, filters, coolers, etc. were not shown in the drawings as it is believed that the specifics of same are well within the knowledge of those of ordinary skill in the art and a description of same is not necessary for practicing or understanding the embodiments of the present invention.