# Patent

## Title
Co-extraction systems for separation and purification of butadiene and isoprene

## Abstract

Co-extraction techniques for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture including butadiene and a C5 hydrocarbon mixture including isoprene are provided. In an exemplary embodiment, a system includes a dimerization heat exchanger, a C5 purification column; an extraction zone including a mainwasher column, a rectifier column and an afterwasher column; a distillation zone; a degassing zone; and an isoprene finishing column. The system can further include a C5 washer column, an absorption column, and a distillation column.

## Background
CROSS REFERENCE TO RELATED APPLICATIONS


    
    
        This application is a National Stage application of PCT/IB2014/062458, WO 2014/203207, filed on Jun. 19, 2014, which claims the benefit of U.S. Provisional Application No. 61/836,799, filed, Jun. 19, 2013, and U.S. Provisional Application No. 61/929,677, filed Jan. 21, 2014, both of which are incorporated by reference in their entirety herein.
    
    




FIELD
The presently disclosed subject matter relates to co-extraction systems and processes for separating and purifying butadiene and isoprene from C4 and C5 hydrocarbon mixtures.
BACKGROUND
Certain technologies for extracting isoprene from a C5 hydrocarbon mixture and/or butadiene from a C4 hydrocarbon mixture are known in the art. For example, U.S. Pat. No. 6,395,953 and U.S. Patent Publication No. 2008/0257711 disclose a process for producing a purified conjugated diene (e.g., isoprene or butadiene) from a petroleum fraction (e.g., a C4 hydrocarbon fraction or C5 hydrocarbon fraction) by extractive distillation. U.S. Pat. No. 4,310,388 describes a process for isolating a conjugated diolefin from a C4- or C5-hydrocarbon mixture by extractive distillation with the aid of a selective solvent. U.S. Pat. No. 3,692,861 discloses a process for separating and purifying isoprene from a C5 hydrocarbon fraction. U.S. Pat. No. 3,436,438 discloses a process of removing acetylenes from a hydrocarbon mixture containing conjugated diolefins (e.g., isoprene or 1,3-butadiene) by using a solvent.
Two or more extraction systems can be required to extract both butadiene and isoprene, with resulting increases in capital cost, utilities, and land usage.
There remains a need in the art for a co-extraction system that can extract both butadiene and isoprene in one system rather than separate systems.
SUMMARY
The presently disclosed subject matter provides co-extraction techniques for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture including butadiene and a C5 hydrocarbon mixture including isoprene. In an exemplary embodiment, a system includes a C5 purification column to receive a C5 hydrocarbon mixture including isoprene and separate the light ends of the C5 hydrocarbon mixture from the heavy ends (C5+) hydrocarbons. The system can further include an extraction zone, a distillation zone, a degassing zone, and an isoprene finishing column to receive a crude isoprene product, where isoprene is purified from the crude isoprene product.
In non-limiting embodiments of the presently disclosed subject matter, the extraction zone can include a mainwasher column to receive the light ends of the C5 hydrocarbon mixture, a C4 hydrocarbon mixture including butadiene, and an extractive solvent. Butadiene and isoprene can be co-extracted from the C4 and C5 hydrocarbon mixtures by using the extractive solvent to provide a crude butadiene product, C4 acetylenes, and a crude isoprene product. The crude butadiene product can include 1,3-butadiene and 1,2-butadiene, cis-2-butene, and trans-2-butene. 1,3-butadiene can be present in a greater amount than 1,2-butadiene, cis-2-butene, and trans-2-butene. The crude isoprene product can include isoprene and 1-pentene. Isoprene can be present in a greater amount than 1-pentene. The extraction zone can also include a rectifier column to receive the crude butadiene product, the crude isoprene product, the extractive solvent, and the C4 acetylenes. The crude butadiene product can be separated from the crude isoprene product, the extractive solvent and the C4 acetylenes in the rectifier column.
In certain embodiments, the extractive solvent can be an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water. In certain embodiments, the extraction zone can further include an afterwasher column coupled to the rectifier column to remove acetylene traces present in the crude butadiene product by using a solvent. The solvent can be n-methyl 2-pyrrolidone.
In non-limiting embodiments of the presently disclosed subject matter, the distillation zone includes a butadiene finishing column to receive the crude butadiene product, where 1,3-butadiene is purified from the crude butadiene product. In some embodiments, the crude butadiene product recovered from the afterwasher column includes propyne. Thus, the distillation zone can further include a propyne column coupled to the afterwasher column to separate propyne from the crude butadiene product.
In non-limiting embodiments of the presently disclosed subject matter, the degassing zone includes a degasser column to receive the crude isoprene product, the extractive solvent, and the C4 acetylenes, where the extractive solvent is separated from the crude isoprene product and the C4 acetylenes. In some embodiments, the degassing zone can further include an acetylene washer column coupled to the degasser column to remove the extractive solvent from the crude isoprene product and the C4 acetylenes.
In certain embodiments the system can further include a selective hydrogenation reactor for the C4 acetylenes in the C4 stream allocated upstream of the butadiene extraction plant to convert acetylenes to butadiene and 1-butene. Such a technology is already available commercially and provided by companies such as BASF, UOP and KBR.
In certain embodiments, the system can further include a dimerization heat exchanger coupled to the C5 purification column to dimerize cyclopentadiene present in the C5 hydrocarbon mixture to dicyclopentadiene. The system can also include a further hydrogenation reactor for converting the remaining undimerized cyclopentadiene to cyclopentene and cyclopentane.
The heavy ends (C5+) hydrocarbons can include, e.g., dicyclopentadiene piperidine, cyclopentane, hexane, 1-hexene, 1,2-hexadiene, methyl-cyclopentadiene, benzene and cyclohexene. The light ends of the C5 hydrocarbon mixture can include, e.g., pentane and isomers thereof, isoprene, pentadiene and isomers thereof, pentene and isomers thereof, and cyclopentene.
The system can further include a C5 washer column that is coupled to the downstream of the C5 purification column. The C5 washer column can receive the light ends of the C5 hydrocarbon mixture from the C5 purification column and an extractive solvent, where the extractive solvent absorbs isoprene from the C5 hydrocarbon mixture. The extractive solvent can include an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water. The C5 washer column can generate an overhead product including C5 components that are not absorbed by the extractive solvent. The overhead product of the C5 washer column can include C5 alkanes (including pentane and isopentane), paraffins and C5 mono-olefins (including pentene and isomers thereof). The C5 washer column can generate a bottom product including the extractive solvent, acetylenes, and C5 di-olefins, which can include pentadienes. The C5 washer column can generate a side product including isoprene. In certain embodiments, the side product of the C5 washer column can further include C5 mono-olefins and di-olefins impurities.
The system can further include an absorption column that is coupled to the downstream of the C5 washer column. The C5 washer column can receive an extractive solvent and the side product of the C5 washer column, where isoprene along with C5 mono-olefins is separated from C5 di-olefins with the aid of the extractive solvent in the absorption column. The extractive solvent can include an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water. The absorption column can generate an overhead product including isoprene and C5 mono-olefins, which can include cyclopentene and pentene isomers. The absorption column can generate a bottom product including C5 diolefins.
The system can further include a distillation column that is coupled to the downstream of the absorption column. The distillation column can receive the overhead product of the absorption column, where isoprene is distilled from the overhead product of the absorption column.
In accordance with another embodiment of the presently disclosed subject matter, processes for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture including butadiene and a C5 hydrocarbon mixture including isoprene are provided. The processes include feeding a C5 hydrocarbon mixture including isoprene to a C5 purification column and separating the light ends of the C5 hydrocarbon mixture from the heavy ends (C5+) hydrocarbons in the C5 purification column. The processes can also include feeding the light ends of the C5 hydrocarbon mixture, a C4 hydrocarbon mixture including butadiene, and an extractive solvent to a mainwasher column and co-extracting isoprene from the light ends of the C5 hydrocarbon mixture and butadiene from the C4 hydrocarbon mixture by using the extractive solvent in the mainwasher column to provide a crude butadiene product, C4 acetylenes, and a crude isoprene product. The extractive solvent can be an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water.
The processes can further include feeding the crude butadiene product, the crude isoprene product, the extractive solvent, and the C4 acetylenes to a rectifier column and separating the crude butadiene product from the crude isoprene product, the extractive solvent and the C4 acetylenes in the rectifier column. In some embodiments, C5 impurities leave the rectifier column with the crude butadiene product. The C5 impurities can include 1-pentene. Furthermore, the processes can include removing acetylene traces present in the crude butadiene product by using a solvent in an afterwasher column. In some embodiments, the crude butadiene product recovered from the afterwasher column includes propyne. Thus, the process can include removing propyne from the crude butadiene product in a propyne column. Furthermore, the processes include feeding the crude butadiene product to a butadiene finishing column and purifying 1,3-butadiene from the crude butadiene product in the butadiene finishing column. In some embodiments, the 1,3-butadiene purified from the butadiene finishing column can have a purity of at least about 99.6% by weight.
In addition, the processes include feeding the crude isoprene product, the extractive solvent and the C4 acetylenes to a degasser column, and separating the extractive solvent from the crude isoprene product and the C4 acetylenes in the degasser column. The processes can also include removing the extractive solvent from the crude isoprene product and the C4 acetylenes in an acetylene washer column. The processes further include feeding the crude isoprene product and the C4 acetylenes to an isoprene finishing column and purifying isoprene from the crude isoprene product and the C4 acetylenes in the isoprene finishing column. The process can include operating the isoprene finishing column at a vacuum of about 50 kiloPascals (kPa) (0.5 atmosphere). In some embodiments, the isoprene purified from the isoprene finishing column has a purity of about 98.6% to about 99.6% by weight.
The processes can further include removing cyclopentadiene present in the C5 hydrocarbon mixture by dimerizing cyclopentadiene to dicyclopentadiene in a dimerization heat exchanger. This can be followed by a selective hydrogenation reaction of the unconverted cyclopentadiene to cyclopentene and cyclopentane.
The process can further include feeding the light ends of the C5 hydrocarbon mixture from the C5 purification column and an extractive solvent to a C5 washer column, where isoprene can be separated from the C5 hydrocarbon mixture by the extractive solvent to generate an overhead product including C5 components that are not absorbed by the extractive solvent, a bottom product including the extractive solvent, C5 di-olefins, and acetylenes, and a side product including isoprene. The side product of the C5 washer column can include C5 mono-olefins and di-olefins impurities. The process can further include feeding the side product of the C5 washer column to an absorption column, where isoprene along with C5 mono-olefins can be separated from C5 di-olefins with the aid of an extractive solvent to generate an overhead product including isoprene and C5 mono-olefins and a bottom product including C5 diolefins and the extractive solvent including the solvent fed to the C5 washer column. The process can further include feeding the overhead product of the absorption column to a distillation column, where isoprene can be distilled from the overhead product of the absorption column.



BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 shows a co-extraction system for separating and purifying butadiene and isoprene in accordance with one non-limiting exemplary embodiment of the disclosed subject matter.
FIG. 2 shows a process for separating and purifying butadiene and isoprene in accordance with one non-limiting exemplary embodiment of the disclosed subject matter.
FIG. 3 shows a co-extraction system for separating and purifying butadiene and isoprene in accordance with one non-limiting exemplary embodiment of the disclosed subject matter.
FIG. 4 shows a process for separating and purifying butadiene and isoprene in accordance with one non-limiting exemplary embodiment of the disclosed subject matter.



DETAILED DESCRIPTION
The presently disclosed subject matter provides co-extracting systems and processes for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture including butadiene and a C5 hydrocarbon mixture including isoprene.
The term “about” or “substantially” means within an acceptable error range for the particular value as determined by one of ordinary skill in the art, which will depend in part on how the value is measured or determined, i.e., the limitations of the measurement system. For example, “about” can mean a range of up to 20%, up to 10%, up to 5%, and or up to 1% of a given value.
As used herein, the term “co-extracting,” “co-extraction,” or “co-extracted” means extracting or extraction of at least two materials or compounds in one process or in one extractive distillation column. For example, the presently disclosed subject matter provides a co-extraction system for butadiene and isoprene, where butadiene and isoprene are extracted in one extractive distillation column, e.g., a mainwasher column.
While technologies for separating and purifying butadiene or isoprene from a C4 or C5 hydrocarbon mixture are known in the art, at least two extraction plants or systems are required to extract both butadiene and isoprene. It is not known in the art to co-extract butadiene and isoprene in one system. The presently disclosed systems and processes can co-extract butadiene and isoprene. Moreover, the extracted butadiene and isoprene have a high purity, e.g., at least about 99.6% by weight, or about 98.6% to about 99.6% by weight.
For the purpose of illustration and not limitation, FIG. 1 shows a co-extraction system 1 in accordance with one embodiment of the disclosed subject matter. FIG. 2 shows a co-extracting process in accordance with one embodiment of the disclosed subject matter. As shown in FIG. 1, the co-extraction system 1 includes a heat treatment/hydrogenation reactor 2. As shown in FIGS. 1 and 2, a C5 hydrocarbon mixture including isoprene is fed to the heat treatment/hydrogenation reactor 2. A C5 hydrocarbon mixture can include isoprene, trans- and cis-1,3-pentadiene, cyclopentadiene (DCPD) as conjugated diolefins, together with pentanes, n-pentenes, isoamylene, cyclopentene, higher acetylenes, methyl pentane isomers, piperylene isomers and methyl cyclobutane. A thermal dimerization is carried out and cyclopentadiene present in the C5 hydrocarbon mixture is dimerized to form di-cyclopentadiene in the heat treatment/hydrogenation reactor 2. The dimerization reaction can be conducted at a temperature of about 90° C. to about 130° C. using medium pressure steam and a pressure of about 100 kPa to about 900 kPa (about 1 barg to about 9 barg). The C5 hydrocarbon mixture is heated in the dimerization heat exchanger for about 5 to about 200 minutes. A substantial amount of cyclopentadiene, e.g., at least about 92% by weight, is removed in this process. Optionally, a further selective hydrogenation can follow to convert any remaining cyclopentadiene to cyclopentene and cyclopentane as discussed in, for example, U.S. Pat. Nos. 3,439,060 and 4,471,153. Therefore all cyclopentadiene present in C5 stream can be converted to dicyclopentadiene, cyclopentene and cyclopentane. Optionally, the hydrogenation reactor 2 can be placed after the C5 purification column.
Example processes for removing cyclopentadiene present in a C5 hydrocarbon mixture by thermal dimerization are disclosed, for example, in U.S. Pat. Nos. 2,768,224, 2,971,036, and 3,692,861. In order to obtain very pure isoprene that is suitable for polymerization to polyisoprene, it can be important to remove cyclopentadiene from a C5 hydrocarbon mixture because cyclopentadiene has a poisoning effect upon the so-called Ziegler-type catalyst and retards polymerization. In addition, cyclopentadiene can clog downstream columns or boilers in the extractive distillation zone if it dimerizes to dicyclopentadiene. The C5 hydrocarbon mixture can be obtained by thermal cracking of a petroleum fraction, e.g., Liquefied Petroleum Gases (“LPG”), naphtha and the like.
As shown in FIGS. 1 and 2, the C5 hydrocarbon mixture is then fed to a C5 purification column 3, where the heavy ends (C5+) hydrocarbons 20 and the light ends of the C5 hydrocarbon mixture 22 are separated. For example, the heavy ends (C5+) hydrocarbons 20 leave from a bottom 24, and the light ends of the C5 hydrocarbon mixture leave from an overhead or top 26, of the C5 purification column 3. Heavy ends (C5+) hydrocarbons include dicyclopentadiene, piperidine, cyclopentane, hexane, 1-hexene, 1,2-hexadiene, methyl-cyclopentadiene, benzene and cyclohexene. Certain C5 hydrocarbons, e.g., piperidine and cyclopentane, can be separated with hydrocarbons having 6 or more carbon atoms from isoprene, because their boiling points are higher than isoprene's. Light ends of a C5 hydrocarbon mixture include pentane and isomers thereof, isoprene, pentene (e.g., 1-pentene) and isomers thereof, pentane and isomers thereof (e.g., isopentane), pentadiene and isomers thereof, and cyclopentene.
As shown in FIGS. 1 and 2, the light ends of the C5 hydrocarbon mixture including isoprene enter an extraction zone 4. The extraction zone 4 can include a mainwasher column 5 and a rectifier column 6. The light ends of the C5 hydrocarbon mixture including isoprene enter the mainwasher column from its top 28. In the C4, stream an optional selective hydrogenation reactor for C4 acetylene can be installed upstream to convert these components to butadiene and 1-butenes using commercially available technologies. A C4 hydrocarbon mixture including butadiene enters the mainwasher column 5 from its bottom 30. The C4 hydrocarbon mixture can be obtained by thermal cracking of a petroleum fraction, e.g., LPG, naphtha and the like. A C4 hydrocarbon mixture can include butanes, 1-butene, isobutene, vinylacetylene, ethylacetylene and 1,2-butadiene, 1,3-butadiene, isobutane, trans-2-butene, cis-2-butene, 1-butyne, and small amounts of C3 hydrocarbons, such as propane, propyne and propadiene, and/or C5 hydrocarbons such as isopentane. In the mainwasher column 5, butadiene and isoprene are co-extracted from the C4 hydrocarbon mixture and the C5 hydrocarbon mixture, respectively, with the aid of an extractive solvent, thereby generating a crude butadiene product and a crude isoprene produce. Acetylenes (e.g., vinylacetylene and ethylacetylene) are also extracted from the C4 hydrocarbon mixture in the mainwasher column 5 by the extractive solvent, and are referred to as “C4 acetylenes.”
The extractive solvent can be conventional solvents, e.g., N-alkyl-substituted cyclic aliphatic acid amides (lactams) having 5 ring members, e.g., N-alkylpyrrolidones (e.g., n-methyl 2-pyrrolidone (“NMP”)), acetonitrile, dimethylformamide, acetone, furfural, butyrolactone, furfuraldehyde, methoxypropionitrile, N-alkyl-substituted lower aliphatic acid amides, e.g., dimethylformamide, diethylformamide, dimethylacetamide, diethylacetamide and formylmorpholine. In one embodiment, the extractive solvent is NMP or an aqueous solution of NMP. NMP, especially an aqueous NMP solution, can be superior to other conventional solvents, because it is non-toxic, non-carcinogenic, and can be treated by conventional biological waste water treatment. In addition, an aqueous NMP solution is non-corrosive, thereby allowing the use of carbon steel as construction material without the need for a corrosion inhibitor. NMP also has low solvent losses due to its resistance to hydrolysis and thermal decomposition as well as its high boiling point, and thus, there will be no vapor losses. Furthermore, NMP is less expensive than other extractive solvents. An aqueous solution of NMP can contain up to 15% by weight of water. In one embodiment, the extractive solution is an aqueous solution of NMP including about 91.7% by weight of NMP and about 8.3% by weight of water.
In some embodiments, the extraction zone 4 includes a flash vessel 15, as shown in FIG. 1. The C4 hydrocarbon mixture can be vaporized in the flash vessel 15 before entering the mainwasher column 5, as shown in FIGS. 1 and 2. The C4 hydrocarbon mixture in gas phase is passed through the mainwasher column 5 counter-currently to the aqueous NMP solution. For extracting 1,3-butadiene from a C4 hydrocarbon mixture, NMP can act as an absorbent over various absorption and desorption stages. For example, 1,3-butadiene is absorbed by NMP while the butenes and butanes present in a C4 hydrocarbon mixture remain in the gas phase. As such, 1,3-butadiene is separated from butenes and butanes. The overhead product of the mainwasher column 5 includes butenes and butanes and is designated as Raffinate-1. The flow rate of the aqueous NMP solution can be adjusted to minimize the amount of 1,3-butadiene in the overhead product (e.g., Raffinate-1) of the mainwasher column 5, e.g., about 0.1% to about 0.2% by weight of 1,3-butadiene in the overhead product. A crude butadiene product, the extractive solvent (e.g., NMP), and C4 acetylenes (e.g., vinylacetylene and ethylacetylene) leave the mainwasher column 5 from its bottom 30. The crude butadiene product includes 1,3-butadiene and its isomers, e.g., 1,2-butadiene. In some embodiments, the crude butadiene product may include small amounts of C4 impurities, e.g., cis-2-butene and trans-2-butene. Processes and technologies for using NMP to extract butadiene from a C4 hydrocarbon mixture are disclosed, e.g., in U.S. Pat. Nos. 4,310,388, and 6,337,429, and German Patent Publication No. DE 2724365, each of which is hereby incorporated by reference in its entirety.
For extracting isoprene from a C5 hydrocarbon mixture, the light ends of the C5 hydrocarbon mixture in liquid phase with a temperature close to that of the extractive solvent (e.g., aqueous NMP solution) enters the mainwasher column 5 from its top 28, as shown in FIG. 2. The light ends of the C5 hydrocarbon mixture are passed through the mainwasher column 5 co-currently to the aqueous NMP solution. Isoprene is extracted from the light ends of C5 hydrocarbon mixture by the extractive solvent (e.g., aqueous NMP solution). A crude isoprene product including isoprene leaves the mainwasher column 5 from its bottom 30. In some embodiments, the crude isoprene product may include a small amount of C5 impurities, e.g., 1-pentene. The C5 hydrocarbons that are not extracted by the extractive solvent, including mainly pentane, isopentane and partly 1-pentene, are stripped from the mainwasher column 5 by the rising vapors of the C4 hydrocarbon mixture. The unextracted C5 hydrocarbons leave the mainwasher column 5 from its top as part of the overhead product of the mainwasher column 5. The flow rate of the aqueous NMP solution can be adjusted to minimize the amount of isoprene in the overhead product of the mainwasher column 5, e.g., about 0.2% to 0.6% by weight of isoprene in the overhead product.
The crude isoprene product, the crude butadiene product, the extractive solvent and C4 acetylenes leave from the bottom 30 of the mainwasher column 5, and enter a rectifier column 6, as shown in FIGS. 1 and 2. In the rectifier column 6, the crude butadiene product is separated from the crude isoprene product, the extractive solvent, and the C4 acetylenes. The crude butadiene product leaves the rectifier column 6 in gas phase as a side draw stream. Most of the C5 impurities (e.g., 1-pentene) leave the rectifier column 6 with the crude butadiene product. The C4 acetylenes, the crude isoprene product and the extractive solvent, with or without traces of C5 impurities (e.g., 1-pentene) leave the rectifier column 6 from its bottom 32 and enter a degassing zone 8, as shown in FIGS. 1 and 2. Therefore, the crude butadiene product and the crude isoprene product are separated in the rectifier column 6.
The extraction zone 4 can further include an afterwasher column 7. After leaving the rectifier column 6, the crude butadiene product in gas phase can be fed to an afterwasher column 7 to remove acetylene traces that may escape with the crude butadiene product in the side draw stream from the rectifier column 6 by a fresh aqueous NMP solution having about 91.7% of NMP and about 8.3% of water. The fresh aqueous NMP solution can be fed to a top 34 of the afterwasher column 7. The crude butadiene product is recovered in the overhead product of the afterwasher column 7. In some embodiments, the overhead product of the afterwasher column 7 includes propyne that is an impurity present in a C4 hydrocarbon mixture. NMP solvent is not present in the overhead due to its high boiling point.
The crude butadiene product enters a distillation zone 9 for further purification. In certain embodiments, the distillation zone 9 includes a propyne column 10. In the propyne column 10, propyne and the crude butadiene product are separated. Propyne is removed as overhead from the propyne column 10 and the crude butadiene product leaves the propyne column 10 from its bottom 36 and enters a butadiene finishing column 11, as shown in FIGS. 1 and 2. In the butadiene finishing column 11, 1,3-butadiene is withdrawn from a top 38 of the column 11 and butadiene isomers (e.g., 1,2-butadiene) as well as other C4 impurities (e.g., trans-2-butene and cis-2-butene) are rejected in the bottom of the column 36. In some embodiments, small amounts of C5 impurities (mainly 1-pentene) and traces of isoprene are rejected in a bottom 40 of an isoprene finishing column 14. A highly pure 1,3-butadiene can be produced in the butadiene finishing column 11. In some embodiments, the purified 1,3-butadiene has a purity of at least 99% by weight, e.g., at least about 99.6% by weight.
The C4 acetylenes, the crude isoprene product and the extractive solvent, with or without traces of C5 impurities (e.g., 1-pentene) leave the rectifier column 6 from its bottom and enter a degassing zone 8, as shown in FIGS. 1 and 2. The degassing zone 8 can include a degasser column 12. The extractive solvent is separated from the crude isoprene product and C4 acetylenes in the degasser column 12. The extractive solvent leaves the degasser column 12 from its bottom 42. The extractive solvent can be recycled to the extraction zone 4. The crude isoprene product reduces polymerization of acetylene by diluting the concentration of acetylene in the degasser column 12, which is operated at a higher temperature than other columns in certain embodiments. In certain embodiments, the degassing zone 8 can include an acetylene washer column 13, as shown in FIGS. 1 and 2. The crude isoprene product and C4 acetylenes, with or without traces of C5 impurities (e.g., 1-pentene), leave the degasser column 12 as a side draw stream in gas phase and enter an acetylene washer column 13, as shown in FIGS. 1 and 2. The acetylene washer column 13 further removes any extractive solvent, which may escape with the crude isoprene and C4 acetylenes from the degasser column 12. In one example, water is added to a top 44 of the acetylene washer column 13 to absorb the extractive solvent into a liquid phase, which is withdrawn from a bottom 46 of the column 13. The crude isoprene product and C4 acetylenes, with or without traces of C5 impurities (e.g., 1-pentene), are dewatered in successive settling vessels, and are fed to an isoprene finishing column 14, as shown in FIGS. 1 and 2. In the isoprene finishing column 14, isoprene is separated from C4 acetylenes and C5 impurities (e.g., 1-pentene). C4 acetylenes and C5 impurities leave as the overhead product of the isoprene finishing column 14. C4 acetylenes can be hydrogenated and used as fuel gas or as cracker feed, or burned in a flare system. Isoprene is withdrawn from the bottom 40 of the isoprene finishing column 14. A highly pure isoprene is produced in the isoprene finishing column 14. In some embodiments, the purified isoprene has a purity of about 98.6% to 99.6% by weight. The isoprene finishing column 14 can be operated under a vacuum of about 0.5 atmosphere to avoid polymerization of acetylenes and isoprene.
In some embodiments, the system can include an isoprene polishing column (not shown) to obtain a higher purified isoprene, e.g., isoprene with a purity of greater than 99.6% by weight. Isoprene can be separated from other heavy hydrocarbons (e.g., dimerized dienes such as traces of dicyclopentadiene and venylcyclohexene) in the isoprene polishing column. The isoprene polishing column can be operated under the same vacuum as that for the isoprene finishing column.
Additionally or alternatively, the system can include a C5 washer column 16. For the purpose of illustration and not limitation, FIGS. 3 and 4 show an exemplary system and a process in accordance with another embodiment of the disclosed subject matter, respectively. As shown in FIGS. 3 and 4, crude C5 can enter a heat exchanger/hydrogenation reactor 82 and exit as a C5 hydrocarbon and enter a C5 purification column 3 with the light ends of the C5 hydrocarbon mixture including isoprene produced or separated from the C5 purification column 3 as shown in FIGS. 1 and 2 can enter a C5 washer column 16 at about the middle of the column as vapor. An extractive solvent 56 can be introduced to a top 50 of the C5 washer column 16 as liquid to absorb the isoprene from the C5 vapors. The extractive solvent can include an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water.
As shown in FIG. 3, the C5 washer column 16 can be fitted with a condenser and a reboiler. The overhead from the C5 washer column can be raffinate stream that includes C5 components that are not absorbed by the extractive solvent, including alkanes (e.g., pentane, isopentane), paraffins and mono-olefins (e.g., pentene (e.g., 1-penetene) and isomers thereof). The bottom product of the C5 washer column can include the extractive solvent along with di-olefins (e.g., pentadienes) and certain acetylenes. An isoprene rich stream 52 can be taken out of the side of the C5 washer column 16 at a location below the middle of the C5 washer column 16 by a vapor draw off stream.
The vapor draw of isoprene can enter an absorption column (17 in FIGS. 3 and 4) close to the bottom tray, and a fresh feed of NMP 54 can be introduced to a top 56 of the column 17. The absorption column 17 can be fitted with a reboiler 70 and a condenser 72. In the absorption column 17, isoprene along with certain mono-olefins such as cyclopentene and certain pentene isomers can be separated from impurities of di-olefins carried in the vapor phase with the isoprene by the fresh solvent fed from the top 58 of this column 17. This extract that includes diolefins and extractive solvent can leave the bottom 60 of the absorption column 17 and can be returned back to the C5 washer column 16. The isoprene along with the remaining C5 hydrocarbon mixture can be withdrawn from the overhead of the absorption column 17 and can enter a distillation column (18 in FIGS. 3 and 4). In the distillation column 18, isoprene can be separated out as the light component from the remaining C5 components, which are heavier than isoprene and can leave the distillation column 18 from its bottom 62. This stream can be remixed with the Pygas aromatic stream of C6+. The purity of the isoprene overhead product can be about 99 wt % or more, e.g., in a range of from about 99.0 wt % to about 99.9 wt %. The column 18 overhead pressure is close to atmospheric and is preferably about 20 kPa to about 100 kPa (about 0.2 barg to about 1 barg).
The bottom stream 74 from the C5 washer column 16 at about 160° C. can be used to heat the boilers 70 of the absorption column 17 and the distillation column 18, and can be used to heat up the propyne column boiler downstream of the butadiene plant, which can save separation energy and ensure heat integration in the butadiene plant. After releasing its heat, the bottom stream 74 from the C5 washer column 16 can then be further cooled to about 38° C. to about 45° C. and can be combined with the extractive solvent stream that is recycled from the butadiene plant and can enter the mainwasher column 5 from the top 28.
C4 impurities can be separated from C5 di-olefins components based on their selectivity in the extractive solvent. The C5 components can enter the rectifier column. As shown in FIGS. 1 and 2, the crude isoprene product (C5 components) along with the C4 acetylenes can be carried in the extractive solvent to the degasser column. As shown in FIGS. 1 and 2, in the degasser column, the C4 acetylenes and the crude isoprene product (C5 components, which include primarily diolefins, e.g., pentadienes isomers) are drawn off as vapor stream out of the extractive solvent. The bottom product of the degasser column can include the extractive solvent that is free of hydrocarbons and can be recycled back as fresh extractive solvent feed. Part of the recycled extractive solvent feed can be used for extracting the C5 hydrocarbon mixture as described above, and then can rejoin the other extractive solvent feed before it enters the mainwasher column 5 of the butadiene plant.
EXAMPLES
The following examples are merely illustrative of the presently disclosed subject matter and they should not be considered as limiting the scope of the presently disclosed subject matter in any way.
Example 1
A commercially available process simulation software tool (PRO-II) was used to construct an in-house model describing the process embodiments given in this disclosure. Process simulation software tools for chemicals processes are known to one of ordinary skill in the art. The in-house model constructed has been used successfully to simulate butadiene extraction process by using an aqueous NMP solution in one butadiene plant. The in-house model was used to simulate the process of co-extraction of butadiene and isoprene in the same plant as described above and as shown in FIGS. 1 and 2.
The in-house model was verified against butadiene extraction plant data where an isoprene spike in the C4 hydrocarbon feed stream to a mainwasher column was measured at different locations around the plant. The results were compared with the model results as shown in Table 1 where isoprene percent level in butadiene plant was taken as 100 units of measure in the feed to the mainwasher column. The results show that the plant data and the results from the model prediction were fairly comparable. This finding consolidates the workable schemes of the embodiments given in the disclosure which are based on simulation model results.







TABLE 1







Isoprene level in downstream units to


isoprene in feed to a mainwasher column









Column
Plant data
Model prediction












Acetylene washer column overhead
80%
88.5%


Mainwasher column overhead
 8%
6.4%


Afterwasher column overhead
5.4% 
5.1%









The results of certain selected streams with main components by using the simulation model are shown in Table 2.







TABLE 2







Stream Composition Wet Bases














C4
C5


Butadiene
Isoprene



hydrocarbon
hydrocarbon

Overhead
purified
purified



mixture
mixture
Overhead
product of
from a
from an



fed to a
fed to a
product of a
an
butadiene
isoprene



mainwasher
mainwasher
mainwasher
afterwasher
finishing
finishing



column
column
column
column
column
column


Components
(wt %)
(wt %)
(wt %)
(wt %)
(wt %)
(wt %)
















propyne
0.0316


0.0375




propadiene
3.6429E−03


butane
5.8969

11.6103


isobutane
1.2072

2.3768


1-butene
12.5472

24.7040


isobutene
14.7248
0.1829
29.0449


trans-2-
6.8850

13.5556


butene


cis-2-butene
3.2380

6.2308
0.1282
0.0542


1,3-butadiene
53.7831

0.2000
93.0610
99.8241


1,2-butadiene
0.1752

0.2526
0.0821


1-butyne
0.1323


vinylacetylene
0.8051


pentane

24.9004
7.2805


isoprene

43.9165
0.5349
0.5766

98.8350


1-pentene

26.5482
1.7506
5.3298


isopentane
0.5401
4.4479
2.3639


butadiene
0.0251




0.4521


dimers









Example 2
The simulation model used in Example 1 was applied to obtain results for the process as depicted shown in FIGS. 3 and 4 to simulate isoprene/butadiene co-extraction using an aqueous NMP. The results of certain selected streams with main components are shown in Table 3 below.







TABLE 3







Stream Composition













C5

Bottom
Feed to
Isoprene



hydrocarbon
Overhead
product of C5
absorption 1 from
purified from



mixture fed to
product of
washer column
vapor draw of
absorption



a C5 washer
a C5 washer
going to main-
C5 washer
column 2



column
column
washer column
column
overhead


Components
(wt %)
(wt %)
(wt %)
(wt %)
(wt %)















1-butene
2.4637
3.4453





isobutene
0.6358
0.8891


trans-2-butene
0.3576
0.5001


cis-2-butene
0.3576
0.5001


1,3-butadiene
10.3318
14.4478
0.9713
1.8987


pentane
36.7966
51.4557


isoprene
15.8949
0.8335

62.0872
99.9548


1-pentene
2.4637
3.4451


isopentane
16.2130
22.6720


neopentane
0.1590
0.2223


Trans2-pentene
0.3576
0.4998

1.5838E−03
2.5183E−03


Cis2-pentene
0.3576
0.4999

3.3610E−03
5.1660E−03


1,2-pentadiene
4.7266
1.3125E−03


Cis-1,3-pentadiene
2.5410
2.9865E−06
0.4582
5.7895


Trans1,3-pentadiene
2.5419
2.6229E−06
0.4587
10.9696


cyclopentene
3.8011
3.4060E−04

16.6834


NMP


90.0218


Water


8.0832









The systems and methods disclosed herein include at least the following embodiments:
Embodiment 1
A co-extraction system for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture comprising butadiene and a C5 hydrocarbon mixture comprising isoprene, comprising: (a) a C5 purification column to receive a C5 hydrocarbon mixture comprising isoprene and separate the light ends of the C5 hydrocarbon mixture from the heavy ends (C5+) hydrocarbons; (b) an extraction zone, comprising: (i) a mainwasher column to receive the light ends of the C5 hydrocarbon mixture, a C4 hydrocarbon mixture comprising butadiene, and an extractive solvent, wherein butadiene and isoprene are co-extracted from the C4 and C5 hydrocarbon mixtures by using the extractive solvent to provide a crude butadiene product, C4 acetylenes, and a crude isoprene product; and (ii) a rectifier column to receive the crude butadiene product, the crude isoprene product, the extractive solvent, and the C4 acetylenes, wherein the crude butadiene product is separated from the crude isoprene product, the extractive solvent, and the C4 acetylenes; (c) a distillation zone, comprising a butadiene finishing column to receive the crude butadiene product, wherein 1,3-butadiene is purified from the crude butadiene product; (d) a degassing zone, comprising a degasser column to receive the crude isoprene product, the extractive solvent, and the C4 acetylenes, wherein the extractive solvent is separated from the crude isoprene product and the C4 acetylenes; and (e) an isoprene finishing column to receive the crude isoprene product and the C4 acetylenes, wherein isoprene is purified from the crude isoprene product and the C4 acetylenes.
Embodiment 2
The system of embodiment 1, wherein the extractive solvent comprises an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water.
Embodiment 3
The system of embodiment 1 or embodiment 2, further comprising a dimerization heat exchanger coupled to the C5 purification column to dimerize cyclopentadiene present in the C5 hydrocarbon mixture to dicyclopentadiene.
Embodiment 4
The system of any of embodiments 1 to 3, wherein the crude butadiene product comprises 1,3-butadiene, 1,2-butadiene, cis-2-butene, and trans-2-butene.
Embodiment 5
The system of embodiment 4, wherein 1,3-butadiene is present in a greater amount than 1,2-butadiene, cis-2-butene, and trans-2-butene.
Embodiment 6
The system of any of embodiments 1 to 5, wherein the crude isoprene product comprises isoprene and 1-pentene.
Embodiment 7
The system of embodiment 6, wherein isoprene is present in a greater amount than 1-pentene.
Embodiment 8
The system of any of embodiments 1 to 7, the extraction zone further comprises (iii) an afterwasher column coupled to the rectifier column to remove acetylene traces present in the crude butadiene product by using a solvent.
Embodiment 9
The system of embodiment 8, wherein the solvent is n-methyl 2-pyrrolidone.
Embodiment 10
The system of embodiment 8, wherein the crude butadiene product recovered from the afterwasher column comprises propyne.
Embodiment 11
The system of embodiment 8, wherein the distillation zone further comprises a propyne column coupled to the afterwasher column to separate propyne from the crude butadiene product.
Embodiment 12
The system of any of embodiments 1 to 11, wherein the degassing zone further comprises an acetylene washer column coupled to the degasser column to remove the extractive solvent from the crude isoprene product and the C4 acetylenes.
Embodiment 13
The system of any of embodiments 1 to 12, wherein the heavy ends (C5+) hydrocarbons comprise piperidine, cyclopentane, hexane, 1-hexene, 1,2-hexadiene, methyl-cyclopentadiene, benzene and cyclohexene.
Embodiment 14
The system of embodiment 13, wherein the heavy ends (C5+) hydrocarbons comprise dicyclopentadiene.
Embodiment 15
The system of any of embodiments 1 to 14, wherein the light ends of the C5 hydrocarbon mixture comprise pentane and isomers thereof, isoprene, pentene and isomers thereof, pentadiene and isomers thereof, and cyclopentene.
Embodiment 16
The system of any of embodiments 1 to 15, further comprising a C5 washer column that is coupled to the downstream of the C5 purification column and receives the light ends of the C5 hydrocarbon mixture from the C5 purification column and an extractive solvent, wherein the extractive solvent absorbs isoprene from the C5 hydrocarbon mixture.
Embodiment 17
The system of embodiment 16, wherein the extractive solvent comprises an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water.
Embodiment 18
The system of embodiment 16, wherein the C5 washer column generates an overhead product comprising C5 components that are not absorbed by the extractive solvent.
Embodiment 19
The system of embodiment 18, wherein the overhead product of the C5 washer column comprises C5 alkanes, paraffins and C5 mono-olefins.
Embodiment 20
The system of embodiment 19, wherein the C5 mono-olefins comprises pentene and isomers thereof.
Embodiment 21
The system of embodiment 19, wherein the C5 alkanes comprises pentane and isopentane.
Embodiment 22
The system of embodiment 16, wherein the C5 washer column generates a bottom product comprising the extractive solvent, C5 di-olefins, and acetylenes.
Embodiment 23
The system of embodiment 22, wherein the di-olefins comprises pentadienes.
Embodiment 24
The system of embodiment 16, wherein the C5 washer column generates a side product comprising isoprene.
Embodiment 25
The system of embodiment 24, wherein the side product of the C5 washer column further comprises C5 mono-olefins and di-olefins impurities.
Embodiment 26
The system of embodiment 25, further comprising an absorption column that is coupled to the downstream of the C5 washer column and receives an extractive solvent and the side product of the C5 washer column, wherein isoprene along with C5 mono-olefins is separated from C5 di-olefins with the aid of the extractive solvent in the absorption column.
Embodiment 27
The system of embodiment 26, wherein the extractive solvent comprises an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water.
Embodiment 28
The system of embodiment 26, the absorption column generates an overhead product comprising isoprene and C5 mono-olefins.
Embodiment 29
The system of embodiment 28, wherein the mono-olefins comprises cyclopentene and pentene isomers.
Embodiment 30
The system of embodiment 26, wherein the absorption column generates a bottom product comprising C5 diolefins and the extractive solvent.
Embodiment 31
The system of embodiment 28, further comprising a distillation column that is coupled to the downstream of the absorption column and receives the overhead product of the absorption column, wherein isoprene is distilled from the overhead product of the absorption column.
Embodiment 32
A process for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture comprising butadiene and a C5 hydrocarbon mixture comprising isoprene, comprising: feeding a C5 hydrocarbon mixture comprising isoprene to a C5 purification column; separating the light ends of the C5 hydrocarbon mixture from the heavy ends (C5+) hydrocarbons in the C5 purification column; feeding the light ends of the C5 hydrocarbon mixture, a C4 hydrocarbon mixture comprising butadiene, and an extractive solvent to a mainwasher column; co-extracting isoprene from the light ends of the C5 hydrocarbon mixture and butadiene from the C4 hydrocarbon mixture by using the extractive solvent in the mainwasher column to provide a crude butadiene product, C4 acetylenes, and a crude isoprene product; feeding the crude butadiene product, the crude isoprene product, the extractive solvent, and the C4 acetylenes to a rectifier column; separating the crude butadiene product from the crude isoprene product, the extractive solvent and C4 acetylenes in the rectifier column; feeding the crude butadiene product to a butadiene finishing column; purifying 1,3-butadiene from the crude butadiene product in the butadiene finishing column; feeding the crude isoprene product, the extractive solvent and the C4 acetylenes to a degasser column; separating the extractive solvent from the crude isoprene product and the C4 acetylenes in the degasser column; feeding the crude isoprene product and the C4 acetylenes to an isoprene finishing column; and purifying isoprene from the crude isoprene product and the C4 acetylenes in the isoprene finishing column.
Embodiment 33
The process of embodiment 32, wherein the extractive solvent comprises an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water.
Embodiment 34
The process of embodiment 32 or embodiment 33, further comprising removing cyclopentadiene present in the C5 hydrocarbon mixture by dimerizing cyclopentadiene to dicyclopentadiene in a dimerization heat exchanger.
Embodiment 35
The process of any of embodiments 32 to 34, further comprising removing cyclopentadiene present in the C5 hydrocarbon mixture by selective hydrogenation of cyclopentadiene to cyclopentene and cyclopentane.
Embodiment 36
The process of any of embodiments 32 to 35, further comprising a C4 selective hydrogenation reactor for acetylenes present in the C4 stream upstream of the butadiene extraction plant.
Embodiment 37
The process of any of embodiments 32 to 36, further comprising removing acetylene traces present in the crude butadiene product by using a solvent in an afterwasher column.
Embodiment 38
The process of any of embodiments 32 to 37, further comprising separating propyne from the crude butadiene product in a propyne column.
Embodiment 39
The process of any of embodiments 32 to 38, further comprising removing the extractive solvent from the crude isoprene product and the C4 acetylenes in an acetylene washer column.
Embodiment 40
The process of any of embodiments 32 to 39, wherein the 1,3-butadiene purified in the butadiene finishing column has a purity of at least about 99.6% by weight.
Embodiment 41
The process of any of embodiments 32 to 40, wherein the isoprene purified in the isoprene finishing column has a purity of about 98.6% to about 99.6% by weight.
Embodiment 42
The process of any of embodiments 32 to 42, comprising operating the isoprene finishing column at a vacuum of about 0.5 atmosphere.
Embodiment 43
The process of any of embodiments 32 to 42, further comprising feeding the light ends of the C5 hydrocarbon mixture from the C5 purification column and an extractive solvent to a C5 washer column.
Embodiment 44
The process of embodiment 43, further comprising absorbing isoprene from the C5 hydrocarbon mixture by the extractive solvent in the C5 washer column to generate an overhead product comprising C5 components that are not absorbed by the extractive solvent, a bottom product comprising the extractive solvent, C5 di-olefins, and acetylenes, and a side product comprising isoprene.
Embodiment 45
The process of embodiment 43, wherein the side product of the C5 washer column comprises C5 mono-olefins and di-olefins impurities.
Embodiment 46
The process of embodiment 44, further comprising feeding the side product of the C5 washer column and an extractive solvent to an absorption column.
Embodiment 47
The process of embodiment 46, further comprising separating isoprene along with C5 mono-olefins from C5 di-olefins with the aid of the extractive solvent in the absorption column to generate an overhead product comprising isoprene and C5 mono-olefins and a bottom product comprising C5 diolefins and extractive solvent.
Embodiment 48
The process of embodiment 47, further comprising feeding the overhead product of the absorption column to a distillation column.
Embodiment 49
The process of embodiment 48, further comprising distilling isoprene from the overhead product of the absorption column in the distillation column.
Although the presently disclosed subject matter and its advantages have been described in detail, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the presently disclosed subject matter as defined by the appended claims. Moreover, the scope of the presently disclosed subject matter is not intended to be limited to the particular embodiments of the process, machine, manufacture, and composition of matter, means, methods and steps described in the specification. As one of ordinary skill in the art will readily appreciate from the disclosure of the presently disclosed subject matter, processes, machines, manufacture, compositions of matter, means, methods, or steps, presently existing or later to be developed that perform substantially the same function or achieve substantially the same result as the corresponding embodiments described herein can be utilized according to the presently disclosed subject matter. Accordingly, the appended claims are intended to include within their scope such modifications.

## Claims

1. A co-extraction system for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture comprising butadiene and a C5 hydrocarbon mixture comprising isoprene, comprising:
(a) a C5 purification column to receive a C5 hydrocarbon mixture comprising isoprene and separate the light ends of the C5 hydrocarbon mixture from the heavy ends (C5+) hydrocarbons;
(b) an extraction zone, comprising:
(i) a mainwasher column to receive the light ends of the C5 hydrocarbon mixture, a C4 hydrocarbon mixture comprising butadiene, and an extractive solvent, wherein butadiene and isoprene are co-extracted from the C4 and C5 hydrocarbon mixtures by using the extractive solvent to provide a crude butadiene product, C4 acetylenes, and a crude isoprene product; and
(ii) a rectifier column to receive the crude butadiene product, the crude isoprene product, the extractive solvent, and the C4 acetylenes, wherein the crude butadiene product is separated from the crude isoprene product, the extractive solvent, and the C4 acetylenes;
(c) a distillation zone, comprising a butadiene finishing column to receive the crude butadiene product, wherein 1,3-butadiene is purified from the crude butadiene product;
(d) a degassing zone, comprising a degasser column to receive the crude isoprene product, the extractive solvent, and the C4 acetylenes, wherein the extractive solvent is separated from the crude isoprene product and the C4 acetylenes; and
(e) an isoprene finishing column to receive the crude isoprene product and the C4 acetylenes, wherein isoprene is purified from the crude isoprene product and the C4 acetylenes.

2. The system of claim 1, wherein the extractive solvent comprises an aqueous solution of n-methyl 2-pyrrolidone having about 91.7% by weight of n-methyl 2-pyrrolidone and about 8.3% by weight of water.

3. The system of claim 1, further comprising a dimerization heat exchanger coupled to the C5 purification column to dimerize cyclopentadiene present in the C5 hydrocarbon mixture to dicyclopentadiene.

4. The system of claim 1, wherein the crude butadiene product comprises 1,3-butadiene, 1,2-butadiene, cis-2-butene, and trans-2-butene and wherein the crude isoprene product comprises isoprene and 1-pentene.

5. The system of claim 1, the extraction zone further comprises (iii) an afterwasher column coupled to the rectifier column to remove acetylene traces present in the crude butadiene product by using a solvent.

6. The system of claim 1, wherein the degassing zone further comprises an acetylene washer column coupled to the degasser column to remove the extractive solvent from the crude isoprene product and the C4 acetylenes.

7. The system of claim 1, wherein the heavy ends (C5+) hydrocarbons comprise piperidine, cyclopentane, hexane, 1-hexene, 1,2-hexadiene, methyl-cyclopentadiene, benzene and cyclohexene and wherein the light ends of the C5 hydrocarbon mixture comprise pentane and isomers thereof, isoprene, pentene and isomers thereof, pentadiene and isomers thereof, and cyclopentene.

8. The system of claim 1, further comprising a C5 washer column that is coupled to the downstream of the C5 purification column and receives the light ends of the C5 hydrocarbon mixture from the C5 purification column and an extractive solvent, wherein the extractive solvent absorbs isoprene from the C5 hydrocarbon mixture.

9. The system of claim 8, wherein the C5 washer column generates an overhead product comprising C5 components that are not absorbed by the extractive solvent wherein the overhead product of the C5 washer column comprises C5 alkanes, paraffins and C5 mono-olefins and wherein the C5 washer column generates a bottom product comprising the extractive solvent, C5 di-olefins, and acetylenes.

10. The system of claim 8, further comprising an absorption column that is coupled to the downstream of the C5 washer column and receives an extractive solvent and the side product of the C5 washer column, wherein isoprene along with C5 mono-olefins is separated from C5 di-olefins with the aid of the extractive solvent in the absorption column.

11. The system of claim 10, the absorption column generates an overhead product comprising isoprene and C5 mono-olefins and wherein the C5 washer column generates a bottom product comprising the extractive solvent, C5 di-olefins, and acetylenes.

12. The system of claim 11, further comprising a distillation column that is coupled to the downstream of the absorption column and receives the overhead product of the absorption column, wherein isoprene is distilled from the overhead product of the absorption column.

13. A process for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture comprising butadiene and a C5 hydrocarbon mixture comprising isoprene, comprising:
feeding a C5 hydrocarbon mixture comprising isoprene to a C5 purification column;
separating the light ends of the C5 hydrocarbon mixture from the heavy ends (C5+) hydrocarbons in the C5 purification column;
feeding the light ends of the C5 hydrocarbon mixture, a C4 hydrocarbon mixture comprising butadiene, and an extractive solvent to a mainwasher column;
co-extracting isoprene from the light ends of the C5 hydrocarbon mixture and butadiene from the C4 hydrocarbon mixture by using the extractive solvent in the mainwasher column to provide a crude butadiene product, C4 acetylenes, and a crude isoprene product;
feeding the crude butadiene product, the crude isoprene product, the extractive solvent, and the C4 acetylenes to a rectifier column;
separating the crude butadiene product from the crude isoprene product, the extractive solvent and C4 acetylenes in the rectifier column;
feeding the crude butadiene product to a butadiene finishing column;
purifying 1,3-butadiene from the crude butadiene product in the butadiene finishing column;
feeding the crude isoprene product, the extractive solvent and the C4 acetylenes to a degasser column;
separating the extractive solvent from the crude isoprene product and the C4 acetylenes in the degasser column;
feeding the crude isoprene product and the C4 acetylenes to an isoprene finishing column; and
purifying isoprene from the crude isoprene product and the C4 acetylenes in the isoprene finishing column.

14. The process of claim 13, further comprising removing cyclopentadiene present in the C5 hydrocarbon mixture by dimerizing cyclopentadiene to dicyclopentadiene in a dimerization heat exchanger.

15. The process of claim 13, further comprising removing cyclopentadiene present in the C5 hydrocarbon mixture by selective hydrogenation of cyclopentadiene to cyclopentene and cyclopentane.

16. The process of claim 13, further comprising separating propyne from the crude butadiene product in a propyne column.

17. The process of claim 13, further comprising removing the extractive solvent from the crude isoprene product and the C4 acetylenes in an acetylene washer column.

18. The process of claim 13, further comprising feeding the light ends of the C5 hydrocarbon mixture from the C5 purification column and an extractive solvent to a C5 washer column.

19. The process of claim 18, further comprising absorbing isoprene from the C5 hydrocarbon mixture by the extractive solvent in the C5 washer column to generate an overhead product comprising C5 components that are not absorbed by the extractive solvent, a bottom product comprising the extractive solvent, C5 di-olefins, and acetylenes, and a side product comprising isoprene.