阅读说明：本技术 Mtbe和烷基化物的共生产 (Co-production of MTBE and alkylate ) 是由 查尔斯·P·利布基 克里斯托弗·D·迪吉利奥 于 2018-12-20 设计创作，主要内容包括：本发明公开了用于共生产甲基叔丁基醚(MTBE)和烷基化物的方法。该方法包括将包含C4烃的烃进料流传递至脱氢单元以生成包含C4烯烃的脱氢流出物。将该脱氢流出物传递至MTBE单元以提供包含C4烯烃和MTBE的混合料流。分离该混合料流以提供MTBE产物料流和包含烯烃的分馏器塔顶料流。将该分馏器塔顶料流传递至烷基化单元以生产包含烷基化物的烷基化产物料流。(A process for the co-production of methyl tert-butyl ether (MTBE) and alkylate is disclosed. The process includes passing a hydrocarbon feed stream comprising C4 hydrocarbons to a dehydrogenation unit to generate a dehydrogenation effluent comprising C4 olefins. The dehydrogenation effluent is passed to an MTBE unit to provide a mixed stream comprising C4 olefins and MTBE. The mixed stream is separated to provide an MTBE product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylate-comprising alkylate product stream.)

1. A process for co-producing a tert-butyl ether compound and an alkylate, comprising:

will contain C₄Passing a hydrocarbon feed stream of hydrocarbons to a dehydrogenation unit to produce a hydrocarbon stream comprising C₄An effluent of dehydrogenation of olefins;

passing the dehydrogenation effluent to a tertiary-butyl ether unit to provide a product comprising C₄A mixed stream of olefins and tertiary butyl ether compounds;

separating the mixed stream to provide a tert-butyl ether product stream and a fractionator overhead stream comprising olefins; and

passing the fractionator overhead stream to an alkylation unit to produce an alkylate-comprising alkylate product stream.

2. The method of claim 1, wherein the tert-butyl ether compound is one of methyl tert-butyl ether (MTBE) or ethyl tert-butyl ether (ETBE).

3. The method of claim 1, further comprising:

passing the alkylate stream to a deisobutanizer to generate a deisobutanizer overhead stream and a deisobutanizer bottoms stream; and

passing the deisobutanizer bottoms stream to a debutanizer to produce a debutanizer overhead stream and the alkylate.

4. The method of claim 3, further comprising:

passing a first portion of the debutanizer overhead stream to an isomerization unit to generate an isomerate stream; and

passing the isomerate stream to the deisobutanizer.

5. The process of claim 4, further comprising passing a second portion of the debutanizer overhead stream to the dehydrogenation unit.

6. The method of claim 1, further comprising passing the hydrocarbon feedstream to an additional deisobutanizer to obtain a C-rich₄An additional deisobutanizer overhead stream of hydrocarbons, and passing the additional deisobutanizer overhead stream to the dehydrogenation unit.

7. The process of claim 1, further comprising passing the dehydrogenation effluent to a selective hydrogenation unit to produce a selective hydrogenation effluent, and passing the selective hydrogenation effluent to an MTBE reactor.

8. The process of claim 1, wherein the alkylation unit is a sulfuric acid alkylation unit.

9. The process of claim 3, further comprising passing a first portion of the deisobutanizer overhead stream to the alkylation unit.

10. The process of claim 3, further comprising recycling a second portion of the deisobutanizer overhead stream to the dehydrogenation unit.

11. The process of claim 10, further comprising controlling an amount of the second portion of the debutanizer overhead stream based on the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit.

12. The process of claim 11, wherein the amount of the second portion of the deisobutanizer overhead stream that is recycled increases as the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit decreases.

13. The process of claim 1, wherein the MTBE fractionation column overhead has an isobutane to olefin ratio ranging from 0.12 to 12.

14. A process for co-producing methyl tert-butyl ether (MTBE) and an alkylate, comprising:

will contain C₄Passing a hydrocarbon feed stream of hydrocarbons to a dehydrogenation unit to produce a hydrocarbon stream comprising C₄An effluent of dehydrogenation of olefins;

passing the dehydrogenation effluent to an MTBE unit to provide a product comprising C₄A mixed stream of olefins and MTBE;

separating the mixed stream to provide an MTBE product stream and a fractionator overhead stream comprising olefins;

passing the fractionator overhead stream to an alkylation unit to produce an alkylate product stream comprising alkylate;

passing the alkylate stream to a deisobutanizer to generate a deisobutanizer overhead stream and a deisobutanizer bottoms stream;

passing a first portion of the deisobutanizer overhead stream to the alkylation unit and recycling a second portion of the deisobutanizer overhead stream to the dehydrogenation unit;

passing the deisobutanizer bottoms stream to a debutanizer to produce a debutanizer overhead stream and the alkylate;

passing a first portion of the debutanizer overhead stream to an isomerization unit to generate an isomerate stream; and

passing the isomerate stream to the deisobutanizer;

wherein the amount of the second portion of the debutanizer overhead stream recycled to the dehydrogenation unit is controlled based on the amount of the first portion of the debutanizer overhead stream passed to the isomerization unit.

15. The process of claim 14, further comprising passing a second portion of the debutanizer overhead stream to the dehydrogenation unit, wherein the amount of the second portion of the debutanizer overhead stream recycled increases as the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit decreases.

16. The method of claim 14, further comprising passing the hydrocarbon feedstream to an additional deisobutanizer to obtain a C-rich₄An additional deisobutanizer overhead stream of hydrocarbons, and passing the additional deisobutanizer overhead stream to the dehydrogenation unit.

17. The process of claim 14, further comprising passing the dehydrogenation effluent to a selective hydrogenation unit to produce a selective hydrogenation effluent, and passing the selective hydrogenation effluent to an MTBE reactor.

18. The method of claim 14, wherein the alkylation unit is a sulfuric acid alkylation unit.

19. An apparatus for co-producing a tertiary butyl ether compound and an alkylate, comprising:

a dehydrogenation unit for the dehydrogenation of a hydrocarbon stream comprising C₄Dehydrogenation of a hydrocarbon feed stream of hydrocarbons to produce a product stream comprising C₄An effluent of dehydrogenation of olefins;

a tert-butyl ether unit in fluid communication with the dehydrogenation effluent line to provide a product stream comprising C₄A mixed stream of olefins and tertiary butyl ether compounds;

a tertiary-butyl ether fractionation column in fluid communication with the tertiary-butyl ether unit for separating the mixed stream to provide a tertiary-butyl ether product stream and a fractionator overhead stream in a fractionator overhead line comprising olefins; and

an alkylation unit in fluid communication with the tert-butyl ether fractionation column to produce an alkylate product stream comprising alkylate.

20. The apparatus of claim 19, the apparatus further comprising:

a deisobutanizer in fluid communication with the alkylation unit to generate a deisobutanizer overhead stream in a deisobutanizer overhead line and a deisobutanizer bottoms stream in a deisobutanizer bottoms line;

a debutanizer column in fluid communication with the deisobutanizer column bottom line to generate a debutanizer column top stream and the alkylate in a debutanizer column top line; and

an isomerization unit in fluid communication with the debutanizer column to generate an isomerate stream and in communication with the deisobutanizer column.

Technical Field

The present invention relates to a process for integrating a methyl tert-butyl ether (MTBE) unit with an alkylation unit to co-produce MTBE and alkylate.

Background

A process for converting paraffins to olefins involves passing a normal paraffin stream over a high selectivity catalyst, where the normal paraffins are dehydrogenated to the corresponding mono-olefins. The dehydrogenation reaction is effected under mild operating conditions, thereby minimizing feedstock losses.

A typical process involves the use of a radial flow reactor that contacts a paraffinic feedstock with a dehydrogenation catalyst under reaction conditions. For example, C can be₂To C₁₁Typical linear paraffins in the range are dehydrogenated to produce olefins for use as monomers in polymer formation, or as plasticizers, or for use in the conversion of C₁₀To C₁₄Dehydrogenation of paraffins in the range to produce linear olefins for the production of Linear Alkylbenzenes (LAB), and for the dehydrogenation of C₁₂To C₁₇Paraffins in the range are dehydrogenated to produce detergent alcohols or olefin sulfonates.

As an example, in sulfuric acid alkylation, it is preferred to employ linear C₄Olefins are used as feedstock because alkylation with n-butenes and isobutane produces higher octane alkylate which yields high octane gasoline. Typically, olefins are purchased externally or obtained from internal refinery streams. Changes in feedstock pricing and feedstock availability can lead to interest in first producing the desired linear olefins, followed by subsequent alkylation.

Need to make full use of C₄The maximum potential of the raw material. Is required for processing C₄A process and apparatus for feedstock that can be adjusted to change product slate to meet changing product requirements. Other desirable features and characteristics of the present subject matter will become apparent from the subsequent detailed description of the subject matter and the appended claims, taken in conjunction with the accompanying drawings and this background of the subject matter.

Disclosure of Invention

Various embodiments of new apparatus and processes for the co-production of tertiary butyl ether compounds and alkylate have been developed. The process provides for the co-production of a tertiary butyl ether compound and an alkylate by integrating a tertiary butyl ether unit with an alkylation unit.

According to an exemplary embodiment, a process for the co-production of a tert-butyl ether compound and an alkylate is provided, which process comprises reacting a mixture comprising C₄Passing a hydrocarbon feed stream of hydrocarbons to a dehydrogenation unit to produce a hydrocarbon stream comprising C₄An effluent from the dehydrogenation of olefins. Passing the dehydrogenation effluent to a tertiary-butyl ether unit to provide a product comprising C₄A mixed stream of olefins and tertiary butyl ether compounds. The mixed stream is separated to provide a tert-butyl ether product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylate-comprising alkylate product stream.

According to another exemplary embodiment, a process for the co-production of methyl tert-butyl ether (MTBE) and alkylate is provided, which process comprises subjecting a feedstock comprising C₄Passing a hydrocarbon feed stream of hydrocarbons to a dehydrogenation unit to produce a hydrocarbon stream comprising C₄An effluent from the dehydrogenation of olefins. Passing the dehydrogenation effluent to an MTBE unit to provide a product comprising C₄A mixed stream of olefins and MTBE. The mixed stream is separated to provide an MTBE product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylate-comprising alkylate product stream. The alkylate stream is passed to a deisobutanizer to produce a deisobutanizer overhead stream and a deisobutanizer bottoms stream. Passing a first portion of the deisobutanizer overhead stream to the alkyl groupA conversion unit, and recycling a second portion of the deisobutanizer overhead stream to the dehydrogenation unit. The deisobutanizer bottoms stream is passed to a debutanizer to produce a debutanizer overhead stream and alkylate. A first portion of the debutanizer overhead stream is passed to an isomerization unit to generate an isomerate stream. Passing the isomerate stream to the deisobutanizer, wherein an amount of a second portion of the deisobutanizer overhead stream recycled to the dehydrogenation unit is controlled based on an amount of the first portion of the debutanizer overhead stream passed to the isomerization unit.

According to an exemplary embodiment, there is provided an apparatus for co-producing a tert-butyl ether compound and an alkylate, comprising a dehydrogenation unit for co-producing a mixture comprising C₄Dehydrogenation of a hydrocarbon feed stream of hydrocarbons to produce a product stream comprising C₄An effluent from the dehydrogenation of olefins. Fluidly connecting a tertiary-butyl ether unit with a dehydrogenation unit to provide a product comprising C₄A mixed stream of olefins and tertiary butyl ether compounds. A tertiary-butyl ether fractionation column is in fluid communication with the tertiary-butyl ether unit for separating the mixed stream to provide a tertiary-butyl ether product stream and a fractionator overhead stream in a fractionator overhead line that includes olefins. An alkylation unit is in communication with the tert-butyl ether fractionation column to produce an alkylation product stream comprising alkylate.

These and other features, aspects, and advantages of the present disclosure are further explained by the following detailed description, drawings, and appended claims.

Drawings

Various embodiments are described below in conjunction with the following drawing figures, wherein like numerals denote like elements.

Fig. 1 illustrates the integration of a dehydrogenation unit and an alkylation unit according to one embodiment of the present disclosure.

Fig. 2 shows integration of a dehydrogenation unit and an alkylation unit according to another embodiment of the present disclosure.

Skilled artisans will appreciate that elements in the figures are illustrated for simplicity and clarity and have not necessarily been drawn to scale. For example, the dimensions of some of the elements in the figures may be exaggerated relative to other elements to help improve understanding of various embodiments of the present disclosure. Also, common and well-understood elements that are useful or necessary in a commercially feasible embodiment may not be depicted in order to facilitate a less obstructed view of these various embodiments of the present disclosure.

Detailed Description

Various embodiments herein relate to processes for co-producing a tert-butyl ether compound (tertiary-butyl ether compound or tertiary-butyl ether compound) and an alkylate. As used herein, the term "stream" may include various hydrocarbon molecules such as linear, branched, or cyclic alkanes, alkenes, alkadienes, and alkynes, and optionally other substances such as gases, e.g., hydrogen, or impurities such as heavy metals, as well as sulfur and nitrogen compounds. The stream may also include aromatic hydrocarbons and non-aromatic hydrocarbons. Further, the hydrocarbon molecule may be abbreviated as C₁、C₂、C₃... Cn, where "n" represents the number of carbon atoms in one or more hydrocarbon molecules. In addition, the superscript "+" or "-" may be used with one or more hydrocarbon symbols of the abbreviation, e.g., C₃₊Or C_3-Which includes one or more hydrocarbons abbreviated. By way of example, the abbreviation "C₃₊"means one or more hydrocarbon molecules having three and/or more carbon atoms.

As used herein, the term "unit" may refer to an area that includes one or more items of equipment and/or one or more zones. Equipment items may include one or more reactors or reactor vessels, heaters, exchangers, piping, pumps, compressors, and controllers. In addition, equipment items such as reactors, dryers or vessels may also include one or more zones or sub-zones.

The term "column" means one or more distillation columns for separating the components of one or more different volatile substances. Unless otherwise specified, each column may include a condenser at the top of the column for condensing a portion of the top stream and refluxing it back to the top of the column, and a reboiler at the bottom of the column for vaporizing a portion of the bottom stream and returning it to the bottom of the column. The feed to the column may be preheated. The top pressure is the pressure of the overhead vapor at the column outlet. The bottom temperature is the liquid bottom outlet temperature. Overhead and bottoms lines refer to the net lines to the column from the column downstream of reflux or reboil.

As used herein, the term "overhead stream" may mean a stream withdrawn at or near the top of a vessel (such as a column).

As used herein, the term "bottoms stream" can refer to a stream withdrawn at or near the bottom of a vessel (such as a column).

As used herein, the term "weight percent" may be abbreviated as "weight percent" (wt.%), and the symbol "%" refers to "% by weight" unless otherwise indicated.

As used herein, the term "rich" may mean that the amount of a compound or class of compounds in a stream is typically at least 50 mole%, and preferably 70 mole%.

As depicted, the process flow lines in the figures are interchangeably referred to as, for example, lines, pipes, branches, distributors, streams, effluents, feeds, products, portions, catalysts, withdrawals, recycles, pumps, discharges, and char dust.

The tert-butyl ether compound produced in the process of the present invention may be any suitable tert-butyl ether compound, including but not limited to methyl tert-butyl ether (MTBE) and ethyl tert-butyl ether (ETBE). MTBE is the most commonly used tert-butyl ether compound. Therefore, for ease of discussion, MTBE will be used. Thus, the apparatus of the present invention as described below will be discussed with respect to MTBE units.

Arriving now at fig. 1, a process and apparatus 100 for co-producing MTBE and alkylate may include a dehydrogenation unit 110, a methyl tert-butyl ether (MTBE) unit 120, an MTBE fractionation column 130, an alkylation unit 140, a deisobutanizer 150, a debutanizer 160, and an isomerization unit 170. May include C in the pipeline 102₄Passing a hydrocarbon feed stream of hydrocarbons to a dehydrogenation unit to produce a hydrocarbon stream comprising C₄An effluent from the dehydrogenation of olefins. The hydrocarbon feedstream can comprise 10 wt.% to 90 wt.% n-butane and 10 wt.% to 90 wt.% isobutane. A second portion of the debutanizer overhead in line 166 can be recycled to the dehydrogenation unit 110. Can be prepared from dehydrogenationUnit 110 withdraws the dehydrogenation effluent in line 112. The dehydrogenation effluent can be passed to MTBE unit 120 to provide an effluent comprising C in line 122₄A mixed stream of olefins and MTBE. According to exemplary embodiments, the dehydrogenation effluent may be passed to a selective hydrogenation unit (not shown) to generate a selective hydrogenation effluent, which may then be passed to an MTBE unit.

The mixed stream in line 122 can be passed to an MTBE fractionation column 130 for separation of the mixed stream to provide a fractionator overhead stream comprising olefins in line 132 and an MTBE product stream in line 134.

The fractionator overhead stream in line 132 may be passed to alkylation unit 140. The alkylation unit may be a sulfuric acid alkylation unit, an ionic liquid alkylation unit, or the like. An alkylation product stream comprising alkylate in line 142 is withdrawn from alkylation unit 140.

The alkylate stream in line 142 may then be passed to deisobutanizer 150 to produce a deisobutanizer overhead in line 152 and a deisobutanizer bottoms in line 158. The deisobutanizer overhead stream in line 152 can be passed to the alkylation unit 140. According to an exemplary embodiment as shown in fig. 1, a first portion of the deisobutanizer overhead stream in line 154 may be passed to the alkylation unit 140. In addition, a second portion of the deisobutanizer overhead stream in line 156 can be passed to the dehydrogenation unit 110. The deisobutanizer bottoms stream in line 158 can be passed to a debutanizer 160 to produce a debutanizer overhead stream in line 162 and alkylate product in line 168. A first portion of the debutanizer overhead stream in line 164 can be passed to an isomerization unit 170. The isomerization unit may be C₄An isomerization unit. A second portion of the debutanizer overhead stream in line 166 can be passed to the dehydrogenation unit 110. In the present disclosure as discussed above, the amount of the second portion of the debutanizer overhead stream 156 passed to the dehydrogenation unit 110 is controlled based on the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit 110 in line 166. In one embodiment, the recycled deisobutanizer overheadThe amount of the second portion of the stream increases as the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit decreases. In one aspect, a control system may be used to control the amount of the second portion of the deisobutanizer overhead stream and the amount of the second portion of the debutanizer overhead stream. The amount transferred to dehydrogenation unit 110 in line 166 can be controlled to vary the amount of MTBE product and alkylate product, and thereby provide flexibility to meet different product slates at different times as desired. For example, in one embodiment, when 100% of the overhead stream in line 162 can be routed to isomerization unit 170 ("max isobutane"), the excess isobutane so produced can be recycled back to dehydrogenation unit 110 ("max MTBE") via line 156. This mode of operation produces high yields of MTBE product. The control system may include a processor and any suitable structure for interacting with one or more sensors and controlling one or more actuators. The control system may, for example, represent a multivariable controller, such as a Robust Multivariable Predictive Control Technology (RMPCT) controller or other type of controller that implements Model Predictive Control (MPC) or other Advanced Predictive Control (APC). As a specific example, each controller may represent a computing device running a real-time operating system.

In some embodiments, various functions described herein may be implemented or supported by a computer program that is formed from computer readable program code and that is embodied in a computer readable medium. The phrase "computer readable program code" includes any type of computer code, including source code, object code, and executable code. The phrase "computer readable medium" includes any type of medium capable of being accessed by a computer, such as Read Only Memory (ROM), Random Access Memory (RAM), a hard disk drive, a Compact Disc (CD), a Digital Video Disc (DVD), a Blu-ray disc, or any other type of memory. "non-transitory" computer-readable media exclude wired, wireless, optical, or other communication links to transmit transitory electrical or other signals. Non-transitory computer readable media include media that can permanently store data as well as media that can store and later rewrite data, such as rewritable optical disks or erasable memory devices.

Referring again to the fractionator overhead stream in line 132, the composition of the fractionator overhead stream is expected to vary from 0.12 to 12 depending on the isobutane to olefin ratio. For example, when the hydrocarbon feedstream contains 90% nC₄The isobutane to olefin ratio was 0.12. In another example, when the hydrocarbon feedstream contains 90% iC₄The isobutane to olefin ratio was 12. In yet another example, when the hydrocarbon feedstream contains 40% iC₄And 60% nC₄When operating in maximum MTBE mode, the isobutane to olefin ratio can vary from 0.5 to 2.6.

An isomerate stream in line 172 is withdrawn from the isomerization unit 170 and may be passed to the deisobutanizer 150.

Turning now to fig. 2, another exemplary embodiment of a method and apparatus 200 for isomerizing hydrocarbons is presented with reference to the method and apparatus 200. Many of the elements in fig. 2 have the same configuration as in fig. l, and have the same corresponding reference numerals and similar operating conditions. Elements in fig. 2 that correspond to elements in fig. 1 but have a different configuration have the same reference numeral as in fig. 1, but are marked with a prime (') symbol. The apparatus and method of fig. 2 is the same as that of fig. 1, except for the following differences noted. According to an exemplary embodiment as shown in fig. 2, the plant 200 comprises an additional deisobutanizer 202. The hydrocarbon feedstream in line 102' can be passed to an additional deisobutanizer 202 to obtain a C-rich stream₄An additional deisobutanizer overhead stream of hydrocarbons, which may then be passed to dehydrogenation unit 110. In addition, a second portion of the debutanizer overhead stream in line 166' can also be passed to an additional deisobutanizer 202. As shown in FIG. 2, an additional deisobutanizer overhead stream rich in butanes is withdrawn in line 204, containing C₅₊Additional deisobutanizer bottoms stream of hydrocarbons is withdrawn in line 206. In addition, a side draw stream (not shown) may also be withdrawn from the additional deisobutanizer 202. The rest of the process is the same as in fig. 1.

Although not shown, the additional deisobutanizer 202 may include a corresponding additional isomerization unit, and the sidedraw stream may be passed to the additional isomerization unit. Additional isomerization units produce streams that are sent back to additional deisobutanizers.

Applicants have found that an integrated process with an MTBE unit as disclosed in the present disclosure allows a user to produce MTBE without adding significant capital expenditure to the integrated dehydrogenation and alkylation process, as MTBE reactors are less expensive relative to dehydrogenation and alkylation units. Furthermore, MTBE has an even higher octane number than alkylate, and can be a premium blending feedstock to achieve a high octane blending product. Moreover, the alkylate product produced now has an even higher octane number, since linear butenes lead to a higher octane number in the sulfuric acid alkylation, since isobutene is reacted off by the MTBE reactor and more linear compounds will be passed to the alkylation unit.

Table 1 shows the flexibility provided by the present solution as disclosed above in changing product composition. Example 1 shows a basic example without MTBE units. Example 2 shows the addition of MTBE units for a feed containing 40 wt% isobutane and 60 wt% n-butane. Example 3 illustrates how the inventive process as disclosed above can vary the amount of MTBE and alkylate produced by adjusting the feed to the isomerization unit. As shown in table 1 below, in example 2, the alkylate was the primary product with some MTBE. However, in example 3 MTBE was the major product. In the table below, the combined feed refers to the feed comprising fresh feed and the portion recycled to the overhead of the debutanizer of the dehydrogenation unit. Thus, the present disclosure as discussed above allows for changing the product without prior fractionation. In addition, the process of the present invention provides control to vary the amount of MTBE product and alkylate product, and thus provides flexibility to meet different product slates at different times as needed.

TABLE 1

Detailed description of the preferred embodiments

While the following is described in conjunction with specific embodiments, it is to be understood that this description is intended to illustrate and not limit the scope of the foregoing description and the appended claims.

A first embodiment of the invention is a process for the co-production of a tert-butyl ether compound and an alkylate, which process comprises reacting a mixture comprising C₄Passing a hydrocarbon feed stream of hydrocarbons to a dehydrogenation unit to produce a hydrocarbon stream comprising C₄An effluent of dehydrogenation of olefins; passing the dehydrogenation effluent to a tertiary-butyl ether unit to provide a product comprising C₄A mixed stream of olefins and tertiary butyl ether compounds; separating the mixed stream to provide a tert-butyl ether product stream and a fractionator overhead stream comprising olefins; and passing the fractionator overhead stream to an alkylation unit to produce an alkylate-comprising alkylate product stream. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the tert-butyl ether compound is one of methyl tert-butyl ether (MTBE) or ethyl tert-butyl ether (ETBE). An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, further comprising passing the alkylate stream to a deisobutanizer to produce a deisobutanizer overhead stream and a deisobutanizer bottoms stream; and passing the deisobutanizer bottoms stream to a debutanizer to produce a debutanizer overhead stream and the alkylate. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, further comprising passing a first portion of the debutanizer overhead stream to an isomerization unit to generate an isomerate stream; and passing the isomerate stream to the deisobutanizer. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, further comprising passing a second portion of the debutanizer overhead stream to the first portion of the debutanizer overhead streamA dehydrogenation unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, further comprising passing the hydrocarbon feedstream to an additional deisobutanizer to obtain the C-rich stream₄An additional deisobutanizer overhead stream of hydrocarbons, and passing the additional deisobutanizer overhead stream to the dehydrogenation unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, further comprising passing the dehydrogenation effluent to a selective hydrogenation unit to produce a selective hydrogenation effluent, and passing the selective hydrogenation effluent to an MTBE reactor. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the alkylation unit is a sulfuric acid alkylation unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, wherein the process further comprises passing a first portion of the deisobutanizer overhead stream to the alkylation unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, wherein the process further comprises recycling a second portion of the deisobutanizer overhead stream to the dehydrogenation unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, further comprising controlling an amount of the second portion of the debutanizer overhead stream based on the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph, wherein the amount of the second portion of the deisobutanizer overhead stream that is recycled increases as the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit decreases. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the MTBE fractionation column overhead has an isobutane to olefin ratio ranging from 0.12 to 12.

A second embodiment of the invention is a process for the co-production of methyl tert-butyl ether (MTBE) and an alkylate, which comprises subjecting a feedstock comprising C₄Passing a hydrocarbon feed stream of hydrocarbons to a dehydrogenation unit to produce a hydrocarbon stream comprising C₄An effluent of dehydrogenation of olefins; passing the dehydrogenation effluent to an MTBE unit to provide a product comprising C₄A mixed stream of olefins and MTBE; separating the mixed stream to provide an MTBE product stream and a fractionator overhead stream comprising olefins; passing the fractionator overhead stream to an alkylation unit to produce an alkylate product stream comprising alkylate; passing the alkylate stream to a deisobutanizer to generate a deisobutanizer overhead stream and a deisobutanizer bottoms stream; passing a first portion of the deisobutanizer overhead stream to the alkylation unit and recycling a second portion of the deisobutanizer overhead stream to the dehydrogenation unit; passing the deisobutanizer bottoms stream to a debutanizer to produce a debutanizer overhead stream and the alkylate; passing a first portion of the debutanizer overhead stream to an isomerization unit to generate an isomerate stream; and passing the isomerate stream to the deisobutanizer; wherein the amount of the second portion of the debutanizer overhead stream recycled to the dehydrogenation unit is controlled based on the amount of the first portion of the debutanizer overhead stream passed to the isomerization unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph, further comprising passing a second portion of the debutanizer overhead stream to the dehydrogenation unit, wherein the amount of the second portion of the deisobutanizer overhead stream that is recycled increases as the amount of the second portion of the debutanizer overhead stream passed to the dehydrogenation unit decreases. Embodiments of the invention are the foregoing in this paragraphEmbodiments of one, any or all of second embodiments in this paragraph up through this paragraph, the method further comprises passing the hydrocarbon feedstream to an additional deisobutanizer to obtain a C-rich stream₄An additional deisobutanizer overhead stream of hydrocarbons, and passing the additional deisobutanizer overhead stream to the dehydrogenation unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph, further comprising passing the dehydrogenation effluent to a selective hydrogenation unit to produce a selective hydrogenation effluent, and passing the selective hydrogenation effluent to an MTBE reactor. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the alkylation unit is a sulfuric acid alkylation unit.

A third embodiment of the present invention is an apparatus for co-producing a tert-butyl ether compound and an alkylate, comprising a dehydrogenation unit for converting a product comprising C₄Dehydrogenation of a hydrocarbon feed stream of hydrocarbons to produce a product stream comprising C₄An effluent of dehydrogenation of olefins; a tert-butyl ether unit in fluid communication with the dehydrogenation effluent line to provide a product stream comprising C₄A mixed stream of olefins and tertiary butyl ether compounds; a tertiary-butyl ether fractionation column in fluid communication with the tertiary-butyl ether unit for separating the mixed stream to provide a tertiary-butyl ether product stream and a fractionator overhead stream in a fractionator overhead line comprising olefins; and an alkylation unit in fluid communication with the tert-butyl ether fractionation column to produce an alkylate product stream comprising alkylate. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the third embodiment in this paragraph, wherein the apparatus further comprises a deisobutanizer in fluid communication with the alkylation unit to generate a deisobutanizer overhead stream in a deisobutanizer overhead line and a deisobutanizer bottoms stream in a deisobutanizer bottoms line; a debutanizer column, said debutanizingA column in fluid communication with the deisobutanizer column bottom line to generate a debutanizer column top stream and the alkylate in a debutanizer column top line; and an isomerization unit in fluid communication with the debutanizer column to generate an isomerate stream and in communication with the deisobutanizer column.

Without further elaboration, it is believed that one skilled in the art can, using the preceding description, utilize the present invention to its fullest extent and can readily ascertain the essential characteristics of the present invention without departing from the spirit and scope thereof, to make various changes and modifications of the invention and to adapt it to various usages and conditions. Accordingly, the foregoing preferred specific embodiments are to be construed as merely illustrative, and not limitative of the remainder of the disclosure in any way whatsoever, and is intended to cover various modifications and equivalent arrangements included within the scope of the appended claims.

In the foregoing, all temperatures are shown in degrees celsius and all parts and percentages are by weight unless otherwise indicated.