RU2619690C2 - Separating components in polymerization - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: method of separating components in the system for producing polymers, comprising the polymerization products flow separation into the gas stream and the polymer stream. The gas stream comprises ethane and unreacted ethylene, gas stream distillation with obtaining the light hydrocarbons stream comprising ethane and unreacted ethylene, bringing the stream of light hydrocarbons in contact with the absorbent solvents system. At least part of the unreacted ethylene from the stream of light hydrocarbons is absorbed by the absorbent solvents system, and the exhausted gases stream is extracted from the absorbent solvents system. The exhausted gases stream comprises ethane, hydrogen, or combinations thereof.

EFFECT: increased separation efficiency.

10 cl, 13 dwg, 3 tbl

Description

[0001] This application is a partial continuation of application for US patent No. 12/905966, filed October 15, 2010, entitled "Improved Ethylene Separation)), which is thereby fully incorporated into the present application by reference for all purposes.

BACKGROUND

Technical field

[0002] The present invention generally relates to the production of polyethylene. More specifically, the present invention relates to systems and methods for increasing the efficiency of producing polyethylene by reducing ethylene losses.

State of the art

[0003] Obtaining polymers, such as polyethylene, from light gases requires highly pure raw materials consisting of monomers and comonomers. Due to the small difference between the boiling points of light gases in such raw materials, the industrial production of high-purity raw materials may require the operation of several distillation columns, high pressures and cryogenic temperatures. For this reason, the energy costs associated with the purification of raw materials represent a significant share of the total cost of production of these polymers. In addition, the infrastructure necessary for the production, maintenance and reuse of high-purity raw materials accounts for a significant portion of the associated capital costs.

[0004] To compensate for some of the costs and maximize production, it may be useful to regenerate and / or reuse any unreacted feed gases, in particular light hydrocarbon reagents such as ethylene. Gases containing unreacted monomers can be separated from the polymer after the polymerization reaction. The polymer is processed, while unreacted monomers are recovered from the gases that regenerate after the polymerization reaction. To carry out such a process, the regenerated gas flows were usually either sent to the cleaning process or redirected to other additional processing stages. In any case, traditional methods for monomer recovery required the use of energetically disadvantageous and expensive processes.

[0005] Accordingly, there is a need for a highly efficient process for separating ethylene from a recycle stream.

SUMMARY OF THE INVENTION

[0006] This application describes a method for separating components in a polymer production system, comprising separating a stream of polymerization products into a gas stream and a polymer stream, the gas stream containing ethane and unreacted ethylene, distilling the gas stream to produce a light hydrocarbon stream containing ethane and unreacted ethylene, bringing the light hydrocarbon stream into contact with an absorbent solvent system, with at least a portion of the unreacted ethylene from the light hydrocarbon stream the ode is absorbed by the absorbent solvent system, and extracting the exhaust gas stream from the absorbent solvent system, wherein the exhaust gas stream contains ethane, hydrogen, or combinations thereof.

[0007] In addition, the present application describes a method for separating components in a polymer production system, comprising separating a stream of polymerization products into a gas stream and a polymer stream, wherein the gas stream contains ethane and unreacted ethylene, distilling the gas stream to produce an intermediate hydrocarbon stream and the first bottoms residue stream, while the intermediate hydrocarbon stream contains ethane, ethylene and isobutene, distillation of the intermediate hydrocarbon stream to produce a light hydrocarbon stream a second bottoms stream, wherein the light hydrocarbon stream contains ethane and ethylene, bringing the light hydrocarbon stream into contact with the absorbent solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorbent solvent system, and extracting the exhaust gas stream from the system absorbent solvents, the exhaust gas stream containing ethane, hydrogen, or combinations thereof.

[0008] The present application also describes a method for separating components in a polymer production system, comprising polymerizing olefin monomers in a first polymerization reactor to produce an intermediate polymerization product stream, separating the intermediate polymerization product stream into an intermediate gas stream and an intermediate polymer stream, wherein the intermediate gas stream contains ethane, unreacted ethylene and hydrogen, and polymerization of the intermediate polymer stream in a second polymerization reactor re.

[0009] The present application also describes a method for separating components in a polymer production system, comprising polymerizing olefin monomers in a first polymerization reactor, separating the intermediate polymerization product stream into an intermediate gas stream and an intermediate polymer stream, wherein the intermediate gas stream contains ethane and unreacted ethylene, polymerizing the intermediate polymer stream in a second polymerization reactor; and introducing an absorber in front of the second polymerization reactor.

[0010] The present application also describes a method for separating components in a polymer production system, comprising polymerizing olefin monomers in a first polymerization reactor to produce an intermediate polymerization product stream, degassing at least a portion of the hydrogen from the intermediate polymerization product stream to obtain a low hydrogen product stream , separation of the product stream with a low hydrogen content into an intermediate gas stream and an intermediate polymer stream, while weft gas stream comprising ethane and unreacted ethylene, and the polymerization intermediate polymer flow in the second polymerization reactor.

[0011] In the above description, the features and technical advantages of the proposed subject matter are described quite broadly for a better understanding of the following detailed description. Various characteristics described above, as well as other features, will be apparent to those skilled in the art after reading the following detailed description of preferred embodiments of the invention with reference to the accompanying drawings.

DESCRIPTION OF DRAWINGS

[0012] For a detailed description of preferred embodiments of the claimed methods and systems will be given links to the accompanying drawings, on which:

[0013] FIG. 1 shows a schematic representation of a first embodiment of a polyethylene production system;

[0014] FIG. 2 shows a schematic representation of a second embodiment of a polyethylene production system;

[0015] FIG. 3 shows a schematic representation of a third embodiment of a polyethylene production system;

[0016] FIG. 4 shows a schematic representation of a fourth embodiment of a polyethylene production system;

[0017] FIG. 5 shows a schematic representation of a fifth embodiment of a polyethylene production system;

[0018] FIG. 6 shows a flowchart of a first embodiment of a method for producing polyethylene;

[0019] FIG. 7 shows a flowchart of a second embodiment of a method for producing polyethylene;

[0020] FIG. 8 shows a flowchart of a third embodiment of a method for producing polyethylene;

[0021] FIG. 9 shows a flowchart of a fourth embodiment of a method for producing polyethylene;

[0022] FIG. 10 is a schematic representation of an embodiment of an absorption reactor configured for short-cycle pressure differential pressure absorption;

[0023] FIG. 11 is a graph illustrating temperature dependence of solubility for ethylene and ethane in an absorbent solvent system;

[0024] FIG. 12 is a schematic illustration of an embodiment of a simulated absorbent system; and

[0025] FIG. 13 is a schematic illustration of an embodiment of a simulated absorbent system.

DETAILED DESCRIPTION OF THE INVENTION

[0026] This application describes systems, installations and methods associated with the production of polyethylene with increased efficiency. Systems, plants and methods are generally associated with separating a first chemical component or compound from a composition formed in the production of polyethylene and containing a first chemical component or compound and one or more other chemical components, compounds or the like.

[0027] FIG. 1 shows the first polyethylene production system (PES) 100. The PES system 100 generally comprises a purifier 102, reactors 104, 106, a separator 108, a software processor, a distillation column 122, an absorption reactor 116, and a processing device 114. According to the embodiments of the PES described in of the present application, various components of the system may be in fluid communication through one or more pipelines (e.g., pipes, pipe system, production lines, etc.) suitable for moving a particular flow, for example, as shown in detail in example onumerovannyh streams in FIG. 1-5, 10, 12-13.

[0028] According to the embodiment of the invention shown in FIG. 1, the feed stream 10 can be transferred to the purifier 102. The cleaned feed stream 11 can be sent from the purifier 102 to one or more reactors 104, 106. In the case where this system contains two or more reactors, the stream 15 can be sent from the reactor 104 to the reactor 106. Hydrogen can be introduced into reactor 106 in stream 21. Polymerization product stream 12 can be directed from one or more reactors 104, 106 to separator 108. Polymer stream 14 can be sent from separator 108 to processor 110. Product stream 16 may exit processor 110. .Gas stream 18 can be directed from the separator 108 to the distillation column 122. From the distillation column 122, a stream of distillation bottoms of the distillation 23 and a side stream 27 can exit. The stream of light hydrocarbons 25 can exit the distillation column 122 and communicate with the absorption reactor 116. The exhaust gas stream 20 can be directed from the absorption reactor 116 to the processing device 114 and the recycle stream 22 can be directed from the absorption reactor 116 to other areas in the system 100, for example to a cleaner 102 through a separator 108. In the case of recirculations Nia cleaner 102 in separator 108 through a recycle stream 22 can be directed from the absorption reactor 116 in separator 108 and flow may be directed from the separator 108 in the cleaner 102.

[0029] FIG. 2 shows a second PES system 200 containing several system components common to the PES 100. According to an alternative embodiment of the invention shown in FIG. 2, the second PES system 200 further comprises a device for removing oxygen 118. Alternatively, the first PES system 100 (shown in FIG. 1), according to the embodiment of the invention shown in FIG. 2, the gas stream 18 can be directed to the oxygen removal device 118. The treated gas stream 26 can be sent from the oxygen removal device 118 to the distillation column 122. It should be understood that embodiments of the claimed subject matter can operate in the presence of the oxygen removal device 118, which may be suitable for gaseous components in the gas stream 18, or in its absence.

[0030] According to an alternative embodiment of the invention shown in FIG. 2, the second PES system 200 further comprises a distillation column 124. According to embodiments of the invention including distillation columns 122 and 124, distillation column 122 can be considered as a first distillation column or a heavy distillation column and distillation column 124 can be considered as a second distillation column or light distillation the column. As shown in FIG. 2, the treated gas stream 26 (and possibly gas stream 18 in the case of embodiments without oxygen removal device 118) can communicate with the distillation column 122. An intermediate hydrocarbon stream 29 can be sent from the distillation column 122 to the distillation column 124. From the distillation column columns 122 may exit a distillation bottoms stream 23. The distillation bottoms stream 33 and possibly a side stream 31 may leave a distillation column 124. A stream of light hydrocarbons 25 may odit from distillation column 124 and enter the absorption reactor 116.

[0031] FIG. 3 depicts a third PES system 300 containing several system components common to PES systems 100 and 200. System components located after the polymerization product stream 12, such as the components shown in FIG. 1 and 2, not shown in FIG. 3; however, it should be understood that embodiments of the invention, such as system 300, may include the components below, according to various described embodiments. According to an alternative embodiment of the invention shown in FIG. 3, the third PES system 300 alternatively comprises a separator 105 located between the reactor 104 and the reactor 106. An absorber can be introduced into the system using stream 35. The stream 35 can be directed with the intermediate polymerization product stream 15 to a separator 105, in which the intermediate polymerization product stream 15 can be divided into the intermediate gas stream 19 and the intermediate polymer stream 17. The intermediate polymer stream 17 can communicate with the reactor 106 from which the polymerization product stream exits 12. The intermediate gas stream 19 may be in communication with the absorption reactor 116, from which the spent stream 20, the absorbent stream 30 and the recycle stream 22 exit. The spent stream 20 can apravit absorption of reactor 116 in a processing device 114 and the recycle stream 22 can be directed from the absorption reactor 116 to other portions of the system 300, as described for the recycle stream 22 with reference to FIG. one.

[0032] FIG. 4 shows a fourth PES 400 system containing several system components common to the PES 300 system. System components located after the polymerization product stream 12, such as those shown in FIG. 1 and 2, not shown in FIG. four; however, it should be understood that embodiments of the invention, such as system 400, may include the components below, according to various described embodiments. According to an alternative embodiment of the invention shown in FIG. 4, the fourth PES system 400 alternatively comprises a separator 126. An intermediate polymerization product stream 15 may exit the reactor 104, which may be in communication with the separator 126. A hydrogen stream 37 may exit the separator 126, and a low hydrogen product stream 39 may be directed from the separator 126 to the separator 105.

[0033] FIG. 5 shows a fifth PES system 500 containing several system components common to PES systems 300 and 400. System components located after the polymerization product stream 12, such as the components shown in FIG. 1 and 2, not shown in FIG. 5; however, it should be understood that embodiments of the invention, such as system 500, may include the components below, according to various described embodiments of the invention. According to an alternative embodiment of the invention shown in FIG. 5, the fifth PPE system 500 further comprises a regenerator 120 (e.g., a desorption vessel). Alternative to the PES systems 100, 200, 300 and 400, according to the embodiment of the invention shown in FIG. 5, the complex stream 28 can be directed from the absorption reactor 116 to the regenerator 120. The recirculated stream 22 can communicate with other areas in the system 500, for example, with the purifier 102, through a separator (as shown in Fig. 1). The flow of regenerated absorbent 30 can be directed from the regenerator 120 to the absorption reactor 116. Although the regenerator 120 is shown in FIG. 5 together with the absorption reactor 116, it is also contemplated that said regenerator can be used in combination with any absorption reactors 116 according to the embodiments of the invention shown in FIG. 1-4. In addition, it should be understood that the absorption reactor 116 shown in FIG. 5 can be configured to function in the absence of a regenerator 120.

[0034] The temperature of the stream 30 in FIG. 5. The temperature of the absorption reactor 116 may depend on the temperature of the gas stream 18, the temperature of the regenerated solvent in stream 30, the heat of dissolution and the heat of reaction. According to the described embodiments of the invention, the specific mass flow rate of the regenerated solvent in the stream 30 may be 50 to 300 times greater than the specific mass flow rate of the gas stream 18. Accordingly, the temperature of the absorption reactor 116 can be highly dependent on the temperature of the regenerated solvent according to the described embodiments of the invention.

[0035] Various embodiments of suitable PES systems have been proposed, and embodiments of the PES method will be described below. One or more embodiments of the PES method can be described with reference to one or more of the systems selected from the PES 100 system, PES 200 system, PES 300 system, PES 400 system and / or PES 500 system. Although this PES method can be described with reference to one or more of the PES system implementation options, such a description should not be construed as limiting. Although the various stages of the processes proposed in this application can be described or shown in a specific order, this order should not be understood as limiting the execution of these processes in any particular order, unless otherwise indicated.

[0036] FIG. 6 shows the first PES 600 process. The PES 600 method generally includes, at step 61, purification of the feed stream, in block 62, polymerizing the monomers of the purified feed stream to produce a polymerization product, in block 63 separating the polymerization product into a polymer stream and a gas stream, in block 64 processing a polymer stream, in block 65, separating at least one gaseous component from the gas stream to produce a recycle stream and a waste stream, and in block 66 burning the waste stream.

[0037] As an example, the first PES process 600 or part thereof can be carried out using the first PES system 100 (for example, shown in Fig. 1). As shown in FIG. 1 and 6, according to one embodiment of the invention, the feed stream 10 may contain a gaseous reactant, in particular ethylene. According to one embodiment of the invention, purification of the feed stream provides a purified stream 11 containing substantially pure monomers (e.g. ethylene monomers), comonomers (e.g. butene-1 comonomers, or combinations thereof). The polymerization of monomers (possibly comonomers) in the purified stream 11 allows to obtain a stream of polymerization products 12, generally containing unreacted monomer (e.g. ethylene), possibly unreacted comonomer (e.g. butene-1), by-products (e.g. ethane, which can represent a by-product formed from ethylene and hydrogen) and a polymerization product (for example, a polymer and possibly a copolymer). Separation of the polymerization product stream 12 makes it possible to obtain a polymer stream 14 (e.g., a polymer, a polyethylene copolymer) and a gas stream 18, generally containing unreacted monomer (e.g., ethylene monomer and any possible comonomer such as butene-1) and various gases (e.g. ethane, hydrogen). Processing the polymer stream 14 allows to obtain a product stream 16. The separation of at least one gaseous component from the gas stream 18 allows to obtain a recycled stream 22, generally containing unreacted ethylene monomer (possibly unreacted comonomer) and an exhaust gas stream 20. According to one embodiment of the invention, separating at least one gaseous component from gas stream 18 may include distilling ethylene from gas stream 18 to produce a light carbohydrate stream odorods 25. According to one embodiment of the invention, the separation of the gas stream 18 may alternatively or additionally absorb ethylene from the gas stream 18 to produce an exhaust gas stream 20 and then isolating the absorbed ethylene to produce a recycle stream 22. The pressure of the recycle stream 22 containing ethylene can be increased. (for example, returning it to the cleaner 102 through the separator 108 to increase the pressure), and re-enter the specified stream in the PES process (for example, the PES process 600). The combustion of the exhaust gas stream 20 can be performed in a flare unit used as a processing device 114.

[0038] FIG. 7 shows the second PES process 700, including several process steps common to the PES process 600. The PES process 700 generally includes in block 71 the purification of the feed stream, in block 72 the polymerization of monomers of the purified feed stream to obtain an intermediate polymerization product, in block 73 the separation of the product the polymerization of the intermediate polymer stream and the intermediate gas stream, in block 74 the polymerization of the monomers (possibly comonomers) of the intermediate polymer stream, in block 75 the separation of at least one gaseous about the component from the intermediate gas stream to obtain a recycle stream and the exhaust stream and in block 76 burning the exhaust stream. According to an alternative embodiment of the invention shown in FIG. 7, steps 63-64 shown in FIG. 6 are replaced by steps 73-75. In general, the process 700 shown in FIG. 7 occurs between reactors 104 and 106, while the process 600 shown in FIG. 6 occurs after reactors 104 and 106.

[0039] As an example, the second PES process 700 or part thereof can be carried out using the third PES system 300 (for example, shown in FIG. 3). As shown in FIG. 3 and 7, according to one embodiment of the invention, the feed stream 10 may contain a gaseous reactant, in particular ethylene. According to one embodiment of the invention, purification of the feed stream provides a purified stream 11 containing substantially pure monomers (e.g., ethylene monomers) and possibly comonomers (e.g., butene-1). Polymerization of the monomers of the purified stream 11 allows to obtain a stream of intermediate polymerization products 15, generally containing unreacted monomer (e.g. ethylene), possibly unreacted comonomer (e.g. butene-1), by-products (e.g. ethane, which may be a by-product, formed from ethylene and hydrogen) and a polymerization product (for example, a polymer and possibly a copolymer). In contrast to the polymerization product stream 12 shown in FIG. 1, which passes after the polymerization reactors 104 and 106, the intermediate polymerization product stream 15 according to the embodiment of the invention shown in FIG. 3 may pass between the polymerization reactor (polymerization reactors) 104 and the polymerization reactor (polymerization reactors) 106. Separating the intermediate polymerization product stream 15 allows the intermediate polymer stream 17 to be obtained, generally containing unreacted ethylene, ethane (which may be a by-product formed from ethylene and hydrogen), a polymer (e.g., polyethylene) and an intermediate gas stream 19 generally containing unreacted monomer (e.g., ethylene monomer ), possibly unreacted comonomer (e.g., butene-1 monomer) and various gases (e.g., ethane, hydrogen). Polymerization of the monomers (possibly comonomers) of the intermediate polymer stream 17 allows the production of a polymerisation product stream 12. The components of the polymerisation product stream 12 can be processed according to the embodiments of systems 100 and 200 shown in FIG. 1 and 2. Separation of at least one gaseous component from the intermediate gas stream 19 allows to obtain a recycle stream 22, generally containing unreacted ethylene monomer (possibly a comonomer), and an exhaust gas stream 20. According to one embodiment of the invention, separating at least one gaseous component from the intermediate gas stream 19 may include the absorption of ethylene from the intermediate gas stream 19 to obtain an exhaust gas stream 20 and then the allocation of absorbor of ethylene to produce a recycle stream 22. You can increase the pressure of the recycle stream 22 containing ethylene and re-introduce it (for example, as shown in Fig. 1) into the PES process (for example, the PES process 700). The combustion of the exhaust gas stream 20 can be performed in a flare unit used as a processing device 114.

[0040] FIG. 8 shows a third PES process 800, which includes several process steps common to the PES process 600 (i.e., blocks 61, 62, 63, 64, 65, and 66). According to an alternative embodiment of the invention shown in FIG. 8, the PES process 800 includes a step 81 for treating the gas stream to produce a treated gas stream and, in block 65 ′, separating at least one gaseous component from the treated gas stream to produce a recirculated stream and an exhaust stream.

[0041] According to one embodiment of the invention, the third PES process 800 or part thereof can be carried out using a second PES system 200 (for example, shown in FIG. 2). Alternative to the embodiments of the invention shown in FIG. 1 and 6, according to the indicated embodiment of the invention shown in FIG. 2 and 8, treating the gas stream 18 allows you to get the treated gas stream 26. According to one embodiment of the invention, treating the gas stream 18 includes removing oxygen from the gas stream 18. Separating at least one gaseous component from the treated gas stream 26 allows for a recirculated stream 22 , generally containing unreacted ethylene monomer (possibly comonomer), exhaust gas stream 20, distillation bottoms stream 23, distillation bottoms stream 33 and side Marketing Stream 31.

[0042] FIG. 9 shows a fourth PES process 900, which includes several process steps common to the PES process 700. According to an alternative embodiment of the invention shown in FIG. 9, the PES process 900 includes a step 91 for processing a gas stream (e.g., intermediate gas stream 19) to produce a treated gas stream. Step 75 shown in FIG. 7 changes in block 75 ′ to separate at least one gaseous component from the treated gas stream to produce a complex stream and an exhaust stream. In block 92, the PES 900 process includes separating the complex stream into an absorbent stream and a recycle stream.

[0043] According to one embodiment of the invention, the fourth PES process 900 or part thereof can be carried out using the fifth PES system 500 (for example, shown in FIG. 5). Alternative to the embodiments of the invention shown in FIG. 3 and 7, according to some embodiments of the invention shown in FIG. 5 and 9, separating at least one gaseous component from the treated gas stream 41 allows the combination of unreacted absorbent monomer (e.g., ethylene absorbent) to be obtained in complex stream 28. According to one embodiment of the invention, separating the complex stream 28 containing the unreacted absorbent monomer comprises separating the absorbed ethylene to produce a recycle stream 22 and an absorbent stream 30. According to the embodiment of the invention shown in FIG. 5 and 9, separating at least one gaseous component from the treated gas stream 26 allows the combination of unreacted comonomer-absorbent (for example, butene-1-absorbent) to be obtained in complex stream 28. According to one embodiment of the invention, separating the unreacted absorbent comonomer in the complex stream 28 comprises isolating the absorbed comonomer to produce a recirculated stream 22 and a regenerated absorbent stream 30.

[0044] According to one or more embodiments of the invention described herein, purification of a feed stream (eg, in block 61 or 71) may include separating undesired compounds and elements from a feed stream containing ethylene to obtain a purified feed stream. According to one embodiment of the invention, the feed stream may comprise ethylene and various other gases, such as, but not limited to, methane, ethane, acetylene, propylene, various other hydrocarbons containing three or more carbon atoms, or combinations thereof. According to one embodiment of the invention, purification of the feed stream may include any suitable method or process, including non-limiting examples of filtration, passage through membranes, chemical interaction with various chemicals, absorption, adsorption, distillation (distillation), or combinations thereof.

[0045] According to the embodiments of the invention shown in FIG. 1-5, purification of the feed stream may include directing the feed stream 10 to the purifier 102. According to one or more embodiments of the invention described in this application, the purifier 102 may comprise a device or installation suitable for purifying one or more gaseous reactants in the feed stream, containing many potentially undesirable gaseous compounds, elements, pollutants, or the like. Non-limiting examples of suitable purifiers 102 may include a filter, a membrane, a reactor, an absorbent, a molecular sieve, one or more distillation columns, or combinations thereof. Purifier 102 may be configured to separate ethylene from a stream containing methane, ethane, acetylene, propane, propylene, water, oxygen, various other gaseous hydrocarbons, various pollutants, and / or combinations thereof.

[0046] According to one embodiment of the invention, purification of the feed stream provides purified feed 11 containing substantially pure ethylene. According to one embodiment of the invention, the purified feed stream may contain any one or more components selected from nitrogen, oxygen, methane, ethane, propane, or combinations thereof, in an amount of less than 25% by weight relative to the total weight of the stream and, alternatively, less than about 10 %, alternatively, less than about 1.0%. As used herein, the term “substantially pure ethylene” refers to a fluid stream containing at least about 60% ethylene, alternatively at least about 70% ethylene, alternatively at least about 80% ethylene, alternatively at least at least about 90% ethylene, alternatively at least about 95% ethylene, alternatively at least about 99% ethylene by weight relative to the total weight of the stream and, alternatively, at least about 99.5% ethylene by weight relative to the total weight of the stream . According to one embodiment of the invention, the feed stream 11 may further comprise trace amounts of ethane, for example, from a recycle stream, as will be described below.

[0047] According to one or more of the embodiments described herein, monomers in a feed stream 11, an intermediate polymerization product stream 15, and an intermediate polymer stream 17 can be polymerized. In one or more embodiments, the polymerization of monomers in purified feed (e.g., at steps 62 and 72) may include carrying out a polymerization reaction between a plurality of monomers by contacting the monomer or monomers with the catalyst system under conditions suitable for forming the polymer. According to one or more of the embodiments described herein, the polymerization of comonomers (e.g., in blocks 62 and 72) in purified feed may include carrying out a polymerization reaction between a plurality of comonomers by contacting the comonomer or comonomers with a catalyst system under conditions suitable for copolymer formation. Similarly, according to one or more of the embodiments described herein, polymerizing monomers in an intermediate polymer stream (e.g., in block 74) may include carrying out a polymerization reaction between a plurality of monomers by contacting the monomer or monomers with the catalyst system under conditions suitable for polymer formation. According to one or more embodiments of the invention described herein, the polymerization of comonomers (e.g., in block 74) in an intermediate polymer stream may include carrying out a polymerization reaction between a plurality of comonomers by contacting the comonomer or comonomers with a catalyst system under conditions suitable for forming copolymer. In the same way, according to one or more of the embodiments described herein, the polymerization of monomers in an intermediate polymerization product may include carrying out a polymerization reaction between a plurality of monomers by contacting the monomer or monomers with the catalyst system under conditions suitable for the formation of the polymer. According to one or more embodiments of the invention described herein, the polymerization of comonomers in an intermediate polymerization product may include carrying out a polymerization reaction between a plurality of comonomers by contacting the comonomer or comonomers with the catalyst system under conditions suitable for forming the copolymer.

[0048] According to the embodiments of the invention shown in FIG. 1-5, the polymerization of the monomers in the purified feed may include directing the feed stream 11 into one or more polymerization reactors or “reactors” 104, 106. According to the embodiments of the invention shown in FIG. 1-2, the polymerization of monomers in the intermediate polymerization product may include directing the flow of the intermediate polymerization products 15 into the polymerization reactor (s) (106). According to the embodiments of the invention shown in FIG. 1-2, the polymerization of monomers in the intermediate polymerization product may include directing the flow of intermediate polymerization products 15 from the polymerization reactor (s) 104 to the polymerization reactor (s) 106. According to the embodiments of the invention shown in FIG. 3-5, the polymerization of monomers in the intermediate polymer stream 17 may include directing the intermediate polymer stream 17 to the polymerization reactor (s) (106). According to the embodiments of the invention shown in FIG. 3-5, the polymerization of monomers in the intermediate polymer stream 17 may include the direction of the intermediate polymer stream 17 from the separator 105 to the polymerization reactor (polymerization reactors) 106.

[0049] According to one embodiment of the invention, any suitable catalyst system can be used. A suitable catalyst system may comprise a catalyst and optionally a co-catalyst and / or activator. Non-limiting examples of suitable catalyst systems include Ziegler-Natta catalysts, Ziegler catalysts, chromium catalysts, chromium oxide catalysts, chromocene catalysts, metallocene catalysts, nickel catalysts, or combinations thereof. Catalytic systems suitable for use in the present invention have been described, for example, in US Pat. No. 7619047 and in US Patent Application Publications No. 2007/0197374, 2009/0004417, 2010/0029872, 2006/0094590 and 2010/0041842, each of which are fully incorporated into the present application by reference.

[0050] According to one or more embodiments of the invention described herein, reactors 104, 106 may comprise any reservoir or combination of reservoirs, respectively, configured to provide a chemical reaction medium (eg, a contact zone) between monomers (eg, ethylene) and / or polymers (eg, an “active” or growing polymer chain) and possibly comonomers (eg, butene-1) and / or copolymers, in the presence of a catalyst to produce a polymer (eg, a polyethylene polymer) and / or copolymer. Although the embodiments of the invention shown in FIG. 1, 2, and 3, illustrate various PES systems containing two series reactors, one of ordinary skill in the art will appreciate that one reactor may be used, alternatively, any suitable number and / or any reactor configuration.

[0051] As used herein, the terms “polymerization reactor” or “reactor” include any polymerization reactor capable of polymerizing olefin monomers or comonomers to produce homopolymers or copolymers. Such homopolymers and copolymers are called resins or polymers. Various types of reactors include reactors that may be called batch reactors, slurry reactors, gas phase reactors, solution polymerization reactors, high pressure reactors, tube or autoclave reactors. Gas phase reactors may include fluidized bed reactors or stepwise horizontal reactors. Suspension reactors may contain vertical or horizontal loops. High pressure reactors may include autoclave or tubular reactors. Types of reactors may include batch or continuous processes. In continuous processes, intermittent or continuous discharge of the product can be used. These processes may also include partial or complete direct recirculation of unreacted monomer, unreacted comonomer and / or diluent.

[0052] The polymerization reactor systems of the present invention may comprise one type of reactor in a system or several reactors of the same or different type. The preparation of polymers in several reactors may include several stages in at least two separate polymerization reactors connected via a transfer stream (s), line (s), unit (s) (e.g., separation tank (s)) and / or device ( devices) (for example, a valve or other mechanism) that make it possible to transfer the resulting polymers from the first polymerization reactor (e.g., reactor 104) to a second reactor (e.g., reactor 106). The required polymerization conditions in one of the reactors may differ from the operating conditions in other reactors. Alternatively, polymerization in multiple reactors may include manually transferring the polymer from one reactor to subsequent reactors for continuous polymerization. Multi-reactor systems may include any combination, including, but not limited to, several loop reactors, several gas reactors, a combination of loop and gas reactors, several high pressure reactors, or a combination of high pressure reactors with loop and / or gas reactors. Several reactors can operate by being connected in series or in parallel.

[0053] According to the embodiments of the invention shown in FIG. 1-5, in the preparation of polymers in several reactors, at least two polymerization reactors 104, 106 connected using one or more devices or plants (for example, using a valve, a continuous outlet valve and / or a continuous outlet mechanism) can be used. According to the embodiments of the invention shown in FIG. 1-2, in the preparation of polymers in several reactors, at least two polymerization reactors 104, 106 connected by one or more streams or lines (e.g., intermediate polymerization product stream 15) can be used. According to the embodiments of the invention shown in FIG. 3-5, when producing polymers in several reactors, at least two polymerization reactors 104, 106 connected via one or more separators (e.g., separator 105 and / or separator 126) via two or more streams (e.g., product stream) can be used intermediate polymerization 15 and intermediate polymer stream 17).

[0054] According to one aspect, the polymerization reactor system may include at least one loop slurry reactor comprising vertical or horizontal loops. The monomer, diluent, catalyst, and possibly any comonomer can be continuously charged into the loop reactor in which the polymerization takes place. In general, continuous processes may include continuously introducing a monomer, optionally a comonomer, a catalyst and a diluent into the polymerization reactor, and continuously removing from the said reactor a suspension containing polymer particles and a diluent. The effluent from the reactor can be quickly evaporated to remove solid polymer from liquids containing diluent, monomer and / or comonomer. Various technologies can be used for this separation stage, including, but not limited to, flash evaporation, which may include any combination selected from heat input and pressure reduction; vortex separation in a cyclone or hydrocyclone; or separation by centrifugation.

[0055] According to one or more embodiments of the invention, the comonomer may contain unsaturated hydrocarbons containing from 3 to 12 carbon atoms. For example, the comonomer may be propene, butene-1, hexene-1, octenes, or combinations thereof.

[0056] A typical suspension polymerization process (also known as a particle formation process) is described, for example, in US Pat.

[0057] In one or more embodiments, suitable diluents used in suspension polymerization include, but are not limited to, the monomer and optionally the comonomer to be polymerized and hydrocarbons, which are liquids under the reaction conditions. Examples of suitable monomeric diluents include, but are not limited to, hydrocarbons such as propane, cyclohexane, isobutane, n-butane, n-pentane, isopentane, neopentane and n-hexane. In embodiments, the comonomer diluents may include unsaturated hydrocarbons containing from 3 to 12 carbon atoms. Examples of suitable comonomer diluents include, but are not limited to, propene, butene-1, hexene-1, octenes, or combinations thereof. Some polymerization reactions carried out in a loop reactor can proceed in volume, with no diluent being used. An example is the polymerization of a propylene monomer described in US Pat. No. 5,453,514, which is hereby incorporated by reference in its entirety.

[0058] According to another aspect, the polymerization reactor may include at least one gas phase reactor. In such a system, a continuous recycle stream containing one or more monomers continuously circulating through a fluidized bed in the presence of a catalyst under polymerization conditions can be used. The recycle stream can be diverted from the fluidized bed and returned to the reactor. At the same time, the polymer product can be removed from the reactor and a new or fresh monomer can be added to replace the polymerized monomer. Similarly, the copolymer product can be removed from the reactor and a new or fresh comonomer can be added to replace the polymerized comonomer, polymerized monomer, or combinations thereof. In such gas-phase reactors, a multi-stage gas-phase polymerization of olefins can be carried out in which olefins are polymerized in the gaseous phase in at least two independent gas-phase polymerization zones when the polymer-containing polymer formed in the first polymerization zone is loaded into the second polymerization zone. One type of gas phase reactor is described in US patent No. 5352749, 4588790 and 5436304, each of which is fully incorporated into the present application by reference.

[0059] According to another aspect, the high pressure polymerization reactor may include a tubular reactor or an autoclave reactor. Tubular reactors can have several zones into which fresh monomer (possibly comonomer), initiators or catalysts can be added. The monomer (possibly comonomer) can be entrained in an inert gaseous stream and introduced into one of the zones of the reactor. Initiators, catalysts and / or catalyst components may be entrained in a gaseous stream and introduced into another zone of the reactor. To carry out the polymerization, the gas flows can be mixed. Heat and pressure can be used appropriately to achieve optimal polymerization reaction conditions.

[0060] In yet another aspect, the polymerization reactor may be a solution polymerization reactor in which a monomer (possibly a comonomer) can be contacted with the catalyst composition by suitable mixing or other methods. A carrier containing an inert organic diluent or an excess of monomer (possibly comonomer) may be used. If necessary, the monomer and / or, possibly, the comonomer may come into contact with the product of the catalytic reaction in the presence or absence of liquid material in the vapor phase. The polymerization zone is maintained at temperatures and pressures that will contribute to the formation of a polymer solution in the reaction medium. To ensure better temperature control and maintain uniformity of the polymerizing mixtures throughout the polymerization zone, mixing can be used. Suitable means are used to dissipate the exothermic heat of the polymerization.

[0061] Polymerization reactors suitable for use in the described systems and processes may further comprise any combination of at least one feed system of at least one catalyst feed system or catalyst components and / or at least one polymer regeneration system. Suitable reactor systems may further include systems for purifying raw materials, storing and preparing the catalyst, extrusion, cooling the reactor, polymer recovery, fractionation, reuse, storage, unloading, laboratory analysis and process control.

[0062] Conditions to be monitored to ensure polymerization efficiency and resin properties include temperature, pressure and concentrations of various reagents. The polymerization temperature can affect the performance of the catalyst, the molecular weight of the polymer and the distribution of molecular weight. A suitable polymerization temperature may be any temperature below the depolymerization temperature according to the Gibbs free energy equation. Typically, such a temperature is, for example, from about 60 ° C to about 280 ° C and from about 70 ° C to about 110 ° C, depending on the type of polymerization reactor.

[0063] Suitable pressures will also vary depending on the type of reactor and polymerization. The pressure in the loop reactor during liquid phase polymerization is usually less than 6.89 MPa gage. (1000 psig). The pressure during gas phase polymerization is usually from about 1.38 to 3.45 MPa gage. (200 to 500 psig). High pressure polymerization in tubular or autoclave reactors generally proceeds at pressures from about 138 to 517 MPa gig. (20,000 to 75,000 psig). Polymerization reactors can also operate in the supercritical region, which is characterized by generally higher temperatures and pressures. Working in the area above the critical point in the pressure / temperature diagram (supercritical phase) can have advantages. According to one embodiment of the invention, the polymerization can take place in an environment with a suitable combination of temperature and pressure. For example, polymerization can occur at pressures ranging from about 3.79 MPa (550 psi) to about 4.48 MPa (650 psi), alternatively, from about 4.14 MPa (600 psi) to about 4.31 MPa (625 psi), and a temperature in the range of about 77 ° C (170 ° F) to about PO ° C (230 ° F), alternatively, from about 91 ° C (195 ° F) to about 104 ° C (220 ° F) .

[0064] To obtain resins with certain physical and mechanical properties, the concentration of various reagents can be controlled. The proposed final product, which will be obtained using a specific resin, and the method for producing such a product determines the desired properties of the resin. Mechanical properties include tests for tensile strength, bending, impact strength, fluidity, stress relaxation and hardness. Physical properties include density, molecular weight, molecular weight distribution, melting point, glass transition temperature, crystal melting point, density, stereoregularity, cracking, long chain branching, and rheological measurements.

[0065] Concentrations and / or partial pressures of the monomer, comonomer, hydrogen, co-catalyst, modifiers, and electron donors are important to provide these resin properties. The comonomer can be used to control the density of the product. Hydrogen can be used to control the molecular weight of the product. Co-catalysts can be used for alkylation, poison removal, and molecular weight control. Modifiers can be used to control product properties, and electron donors affect molecular symmetry, molecular weight distribution, or molecular weight. In addition, the concentration of poisons is minimized, since poisons affect the reactions and properties of the product.

[0066] According to one embodiment of the invention, the polymerization of monomers may include introducing a suitable catalyst system into the first and / or second reactor 104, 106, respectively, to form a slurry. Alternatively, a suitable catalyst system may be located in the first and / or second reactor 104, 106, respectively.

[0067] As shown above, the polymerization of monomers may include selectively manipulating one or more of the conditions of the polymerization reaction to obtain a given polymer product, to obtain a polymer product having one or more desired properties, to achieve the desired efficiency, to achieve the desired yield, etc. . or combinations thereof. Non-limiting examples of such parameters include temperature, pressure, type and / or amount of catalyst or co-catalyst, and concentrations and / or partial pressures of various reagents. In one embodiment, the polymerization of monomers in refined feedstock 52 may include controlling one or more polymerization reaction conditions. In one embodiment, the polymerization of the monomers may include adding ethylene monomer and / or comonomer, such as butene, to the polymerization reactor 106.

[0068] According to one embodiment of the invention, the polymerization of the monomers may include maintaining a suitable temperature, pressure and / or partial pressure (s) during the polymerization reaction, alternatively cyclic by changing the set of suitable temperatures, pressures and / or partial pressure (s) in the process polymerization reactions.

[0069] In one embodiment, the polymerization of monomers may include introducing hydrogen into one or more reactors 104 and 106. For example, in FIG. 1 and 2, it is shown that hydrogen can be introduced into the reactor 106 using stream 21. The amount of hydrogen introduced into the reactor 106 can be adjusted so as to provide a molar ratio of hydrogen to ethylene of 0.001 to 0.1 in the diluent. In the reactor 106, such a molar ratio may be at least 0.004. According to embodiments of the invention, said molar ratio cannot exceed 0.05. The ratio of the concentration of hydrogen in the diluent in the reactor 104 to the concentration of hydrogen in the polymerization reactor 106 may be at least 20, alternatively at least 30, alternatively at least 40, alternatively not more than 300, alternatively not more than 200. Suitable methods and hydrogen concentration control systems are described in US Pat. No. 6,225,421, which is incorporated herein by reference.

[0070] According to one embodiment of the invention, the polymerization of the monomers may include circulation, flow, cyclic motion, mixing, shaking, or combinations thereof of monomers (possibly comonomers), a catalyst system and / or suspension in reactors 104, 106 and / or in between them. According to one embodiment of the invention, when the monomers (possibly comonomers), the catalytic system and / or suspension are circulated, the circulation can occur at a speed (for example, a suspension speed) of from about 1 m / s to about 30 m / s, alternatively from about 2 m / s to about 17 m / s, alternatively from about 3 m / s to about 15 m / s.

[0071] According to one embodiment of the invention, the polymerization of monomers may include adjusting the reactors 104, 106 to produce a multimodal (eg, bimodal) polymer (eg, polyethylene). For example, the resulting polymer can be both a relatively high molecular weight low density polyethylene polymer (HMWLD) and a relatively low molecular weight high density polyethylene polymer (LMWHD). For example, various types of suitable polymers can be characterized as possible polymers with different densities. For example, Type I may be characterized as a polymer having a density in the range from about 0.910 g / cm ³ to about 0.925 g / cm ^3, alternatively, the type II can be characterized as a polymer having a density from about 0.926 g / cm ³ to about 0.940 g / cm ³ , alternatively, type III can be characterized as a polymer with a density of from about 0.941 g / cm ³ to about 0.959 g / cm ³ , alternatively, type IV can be described as a polymer with a density of more than about 0.960 g / cm ³ .

[0072] According to one embodiment of the invention, the polymerization of monomers may include the polymerization of comonomers in one or more polymerization reactors 104, 106.

[0073] According to some embodiments of the invention shown in FIG. 1-5, the polymerization of the monomers of the purified feedstock allows to obtain an intermediate polymerization product stream 15 and / or a polymerization product stream 12. Such an intermediate polymerization product stream 15 and / or a polymerization product stream 12 may generally contain various solids, semi-solids, volatile and non-volatile liquids, gases and their combinations. According to one embodiment of the invention, the intermediate polymerization product stream 15 and / or the polymerization product stream 12 may contain hydrogen, nitrogen, methane, ethylene, ethane, propylene, propane, butane isobutane, pentane, hexane, hexene-1 and heavier hydrocarbons. According to one embodiment of the invention, ethylene may be present in an amount of from about 0.1% to about 15%, alternatively, from about 1.5% to about 5%, alternatively, from about 2% to about 4% by weight relative to the total weight flow. Ethane may be present in an amount of from about 0.001% to about 4%, alternatively, from about 0.2% to about 0.5% by weight relative to the total weight of the stream. Isobutane may be present in an amount of from about 80% to about 98%, alternatively, from about 92% to about 96%, alternatively, about 95% by weight relative to the total weight of the stream.

[0074] Solids and / or liquids may contain a polymer product (eg, polyethylene polymer), often referred to as “polymer dust” at this stage of the PES process. Gases may contain unreacted, gaseous reactive monomers, or possibly comonomers (e.g., unreacted ethylene monomers, unreacted butene-1 monomers), gaseous wastes, gaseous pollutants, or combinations thereof.

[0075] According to one or more embodiments of the invention described herein, separating the polymerization product into a polymer stream and a gas stream (for example, in block 63) may generally include removing any gases from liquids and / or solids (eg, polymer dust) using any suitable means.

[0076] According to the embodiments of the invention shown in FIG. 1-2, the separation of the polymerization product into a polymer stream and a gas stream may include directing a stream of polymerization products 12 to a separator 108.

[0077] According to one embodiment of the invention, gas stream 18 may comprise hydrogen, nitrogen, methane, ethylene, ethane, propylene, propane, butane isobutane, pentane, hexane, hexene-1, and heavier hydrocarbons. According to one embodiment of the invention, ethylene may be present in an amount of from about 0.1% to about 15%, alternatively, from about 1.5% to about 5%, alternatively, from about 2% to about 4% by weight relative to the total weight flow. Ethane may be present in an amount of from about 0.001% to about 4%, alternatively, from about 0.2% to about 0.5% by weight relative to the total weight of the stream. Isobutane may be present in an amount of from about 80% to about 98%, alternatively, from about 92% to about 96%, alternatively, about 95% by weight relative to the total weight of the stream.

[0078] According to one or more embodiments of the invention, the separation of the intermediate polymerization product into an intermediate polymer stream and an intermediate gas stream (eg, in block 73) may generally include the removal of any gases from liquids and / or solid phase (eg, polymer dust) with using any suitable methods.

[0079] According to the embodiments of the invention shown in FIG. 3 and 5, separation of the intermediate polymerization product into the intermediate polymer stream and the intermediate gas stream can be accomplished by one-stage separation, including the direction of the intermediate polymerization products stream 15 to the separator 105.

[0080] According to the embodiments of the invention shown in FIG. 3, separating the intermediate polymerization product into an intermediate polymer stream and the intermediate gas stream may include separating at least one gaseous component from the intermediate polymerization product stream 15. Separating at least one gaseous component from the intermediate polymerization product stream 15 allows the intermediate gas stream 19 to be obtained and intermediate polymer stream 17. The intermediate polymerization product stream 15 may contain hydrogen, ethylene, ethane, polymer, isobutane and whether their combinations. The intermediate gas stream 19 may contain hydrogen, ethylene, ethane, or combinations thereof. The intermediate polymer stream 17 may comprise a polymer, isobutane, or combinations thereof.

[0081] According to the embodiments of the invention shown in FIG. 3, separating the intermediate polymerization product into an intermediate polymer stream and an intermediate gas stream may include lowering the pressure of the intermediate polymerization product to instantly vaporize ethylene, hydrogen, ethane, or combinations thereof. The intermediate polymerization product stream 15 may comprise hydrogen, ethylene, ethane, a polymer, isobutane, or combinations thereof. The separator 105 may create a reduced pressure to separate or rapidly evaporate, ethylene, hydrogen and ethane from the intermediate polymerization product so as to obtain an intermediate gas stream 19 containing hydrogen, ethylene and ethane.

[0082] According to the embodiments of the invention shown in FIG. 5, separating the intermediate polymerization product into an intermediate polymer stream and an intermediate gas stream may include introducing a scavenger upstream of reactor 106. According to embodiments of the invention, the scavenger can reduce the concentration of a component, such as hydrogen. Embodiments of the invention illustrated in FIG. 3 and 5 show that stream 35 can be introduced upstream of reactor 106 using, for example, an intermediate polymerization product stream 15. Alternatively, stream 35 can be introduced into a separator 105 or intermediate polymer stream 17. Stream 35 may comprise an absorber. According to embodiments of the invention, the scavenger may comprise a catalyst. According to embodiments of the invention, the catalyst may be a hydrogenation catalyst. Not wanting to be bound by theory, the scavenger can act in such a way as to consume hydrogen and form ethane, which can reduce the concentration of hydrogen, even to zero concentration. According to embodiments of the invention, the hydrogenation catalyst may have low activity with respect to polymerization of polyethylene. The hydrogenation catalyst may be a metallocene catalyst of the general formula:

Cp ₂ MX _n ,

where Cp represents a substituted cyclopentadienyl group; M is a transition metal from Group IVB vanadium of the periodic table; X represents a halogen or hydrocarbyl group containing from 1 to 10 carbon atoms; and n represents a metal valency of M minus 2. According to embodiments of the invention, the metallocene catalyst may comprise Cp ₂ TiCl ₂ , also known as titanocene dichloride. The metallocene catalyst can be introduced in an amount of from 2 to 50 ppm by weight relative to an inert diluent in the intermediate polymerization product stream 15, alternatively, in an amount of from 2 to 20 ppm.

[0083] According to the embodiments of the invention shown in FIG. 5, lowering the concentration of hydrogen in the stream upstream of the second polymerization reactor 106 by means of an absorber can improve the ability to form a polymer, for example, it is possible to obtain a polymer with a relatively higher molecular weight in the polymerization reactor 106 than in the polymerization reactor 104. For example, according to embodiments of the invention, in which a relatively higher molecular weight polymer is to be obtained in the reactor 106, usually no additional hydrogen is added to the reactor 106, since The increased hydrogen concentration in reactor 106 is generally detrimental to the production of a polymer with a higher molecular weight. In such embodiments, instead of introducing hydrogen into or in front of reactor 106, a hydrogenation catalyst can be introduced. The embodiments of the invention shown in FIG. 3 and 5 demonstrate that the hydrogenation catalyst can be introduced in stream 35 upstream of reactor 106. According to one or more embodiments of the invention, the resulting polymer may comprise polyethylene. According to such embodiments, the Ziegler-Natta catalyst can be used as the polymerization catalyst, and the hydrogenation catalyst introduced through stream 35 may comprise a metallocene catalyst. The amount of metallocene catalyst used may be such that the weight ratio of the metallocene catalyst to the Ziegler-Natta catalyst (i.e., g metallocene / g Ziegler-Natta) can be from about 0.1 to about 2.0, preferably from about 0 25 to about 1.5, more preferably from about 0.5 to 1.0. According to one embodiment of the invention, the metallocene catalyst may comprise a non-bridged metallocene. In one embodiment, the non-bridged metallocene may be titanium bis (cyclopentadienyl) dichloride, also called titanocene dichloride. Suitable hydrogenation catalysts are described in US patent No. 6730751, 6221982 and 6291601, which are incorporated into this application by reference.

[0084] According to the embodiments of the invention shown in FIG. 5, separating the intermediate polymerization product into an intermediate polymer stream and the intermediate gas stream may further include separating at least one gaseous component from the intermediate polymerization product stream. According to such embodiments of the invention, the intermediate polymerization product stream 15 entering the separator 105 may comprise unreacted hydrogen, unconverted ethylene, ethane, polymer, isobutane, or combinations thereof. The intermediate gas stream 19 may comprise hydrogen, ethylene, ethane, or combinations thereof; and the intermediate polymer stream 17 may comprise a polymer, isobutane, or combinations thereof. The amount of ethane in the intermediate gas stream 19 may be greater than the amount of unreacted hydrogen and / or unconverted ethylene.

[0085] According to the embodiments of the invention shown in FIG. 4, separation of the intermediate polymerization product into an intermediate polymer stream and an intermediate gas stream (for example, in block 73) can be accomplished by two-stage separation, including the direction of the intermediate polymerization products stream 15 to the separator 126 and the direction of the product stream with a reduced hydrogen content 39 from the separator 126 to separator 105.

[0086] According to the embodiments of the invention shown in FIG. 4, separating the intermediate polymerization product into an intermediate polymer stream and the intermediate gas stream may include degassing at least a portion of the hydrogen from the intermediate polymerization product. The embodiments of the invention shown in FIG. 4 demonstrate that separator 126 allows streams 37 and 39 to be obtained. Stream 37 may contain remote hydrogen and stream 39 may contain a product with a reduced hydrogen content. The separator 126 can degass at least a portion of the hydrogen from the intermediate polymerization product stream 15 by lowering the pressure. Pressure reduction may occur in the reactor 104 at a temperature less than or equal to the polymerization temperature, alternatively, at a temperature of more than 20 ° C, alternatively at least 40 ° C. The pressure reduction can occur at a pressure lower than the pressure in the reactor 104. The pressure reduction can be less than 1.5 MPa. The pressure reduction may be at least 0.1 MPa. The amount of hydrogen remaining in the reduced hydrogen stream 39 shown in FIG. 4 may be less than 1% by weight relative to the amount of hydrogen initially present in the mixture removed from reactor 104, alternatively, less than 0.5% by weight, alternatively 0% by weight. by weight. Suitable degassing conditions and equipment are described in US Pat. No. 6,225,412, which is incorporated herein by reference.

[0087] According to the embodiments of the invention shown in FIG. 4, separating the intermediate polymerization product into an intermediate polymer stream and an intermediate gas stream may further include separating at least one gaseous component from the product stream with a reduced hydrogen content. According to such embodiments of the invention, the low hydrogen product stream 39 entering the separator 105 may comprise hydrogen, ethylene, ethane, a polymer, isobutane, or combinations thereof. The intermediate gas stream 19 may comprise hydrogen, ethylene, ethane, or combinations thereof; and the intermediate polymer stream 17 may comprise a polymer, isobutane, or combinations thereof. The amount of hydrogen present in the intermediate gas stream 19 shown in FIG. 4 may be less than 1% by weight relative to the amount of hydrogen initially present in the mixture removed from reactor 104, alternatively, less than 0.5% by weight, alternatively 0% by weight. by weight.

[0088] According to one or more of the embodiments described herein, separators 105, 108, and 126 may be configured to separate a stream (eg, an intermediate polymerization product containing polyethylene, a polymerization product containing polyethylene, a product with a reduced hydrogen content, containing polyethylene) for gases, liquids, solids, or combinations thereof. Product streams 12, 15, and 39 may contain unreacted, gaseous monomers, or possibly comonomers (e.g., unreacted ethylene monomers, unreacted butene-1 monomers), gaseous waste, and / or gaseous pollutants. According to the embodiments of the invention shown in FIG. 4, the intermediate polymerization product stream 15 may contain hydrogen. According to the embodiments of the invention shown in FIG. 1-2, the stream of polymerization products 12 may contain hydrogen. As used herein, the term “unreacted monomer,” for example ethylene, refers to monomer that was introduced into the polymerization reactor during the polymerization reaction but was not incorporated into the polymer. As used herein, the term “unreacted comonomer,” for example, butene-1, refers to a comonomer that was introduced into the polymerization reactor during the polymerization reaction but was not incorporated into the polymer.

[0089] According to one embodiment of the invention, the separators 105, 108 and / or 126 may be a vapor-liquid separator. Suitable examples of such a separator may include a distillation column, an evaporation tank, a filter, a membrane, a reactor, an absorbent, an adsorbent, a molecular sieve, or combinations thereof. According to one embodiment of the invention, the separator comprises an evaporation tank. Not wishing to be bound by theory, such an evaporation tank may comprise a reservoir configured to vaporize and / or remove components with a low specific vapor pressure from a high temperature and / or high pressure fluid. The separators 105, 108 and / or 126 may be designed so that the inlet stream can be divided into a liquid stream (e.g., a condensate stream) and a gas stream (e.g., steam). The liquid or condensate stream may contain a reaction product (for example, polyethylene, often called "polymer dust"). The gas stream or vapor may contain volatile solvents, gaseous, unreacted monomers and / or possibly comonomers, exhaust gases (secondary reaction products, such as pollutants, etc.) or combinations thereof. The separators 105, 108 and 126 can be made in such a way that the feed stream quickly evaporates under the influence of heat, pressure reduction, or both, so that the enthalpy of the stream increases. Such a process can be carried out using a heating device, a vapor line heater, various other processes widely known in the art, or combinations thereof. For example, a heating device with an evaporation line containing a double pipe can exchange heat with hot water or steam. Such a heater with an evaporation line allows you to increase the temperature of the stream while reducing its pressure.

[0090] According to one or more embodiments of the invention, the separation of the polymerization product into a polymer stream and a gas stream or the separation of the intermediate polymerization product into an intermediate polymer stream and an intermediate gas stream may include distillation, evaporation, flash evaporation, filtration, sieving through membranes, absorption, adsorption polymerization product or a combination thereof. According to some embodiments of the invention shown in FIG. 1-2, the separation of the polymerization product into a polymer stream and a gas stream makes it possible to obtain a gas stream 18 and a polymer stream 14. According to some embodiments of the invention shown in FIG. 3-5, the separation of the intermediate polymerization product into an intermediate polymer stream and an intermediate gas stream allows to obtain an intermediate gas stream 19 and an intermediate polymer stream 17.

[0091] According to one or more embodiments of the invention described herein, processing a polymer stream (eg, in block 64) includes any suitable process or series of processes designed to produce a polymer product that may be suitable for commercial or industrial use, storage , transportation, additional processing, or combinations thereof.

[0092] According to the embodiments of the invention shown in FIG. 1-2, processing the polymer stream may include directing the polymer stream 14 to the processor 110. The processor 110 may be configured to implement suitable processing methods, non-limiting examples of which include cooling, injection molding, melting, granulation, blow molding, extrusion molding, rotational molding, thermoforming, injection molding, etc. or combinations thereof. Various additives and modifiers can be added to the polymer to ensure better processing during the production process and to give the necessary properties to the final product. Non-limiting examples of such additives may include surface modifiers, such as anti-friction additives, release agents, tackifiers; antioxidants such as primary and secondary antioxidants; pigments process enhancing agents such as waxes / oils and fluoroelastomers; and special additives such as flame retardants, antistatic agents, absorbents, absorbers, odor improvers, and disintegrating agents.

[0093] According to one embodiment of the invention, processor 110 may be configured to produce a suitable polymer product. Non-limiting examples of suitable polymeric products that can be obtained by such processing include films, powders, granules, resins, liquids, or any other suitable form, as will be appreciated by those skilled in the art. Said suitable products may be used, for example, in one or more different consumer or industrial products. For example, a polymer product can be used in any one or more different products, including, but not limited to, bottles, barrels, toys, household containers, utensils, film products, tanks, fuel tanks, pipes, geomembranes and facings. According to a specific embodiment of the invention, the processor is configured to form granules for transporting consumer products to the manufacturer. For example, according to some embodiments of the invention shown in FIG. 1-2, processing the polymer stream allows to obtain a polymer product 16 (for example, granular polyethylene).

[0094] According to one or more embodiments of the invention described herein, treating a gas stream (for example, in block 81) and treating an intermediate gas stream (for example, in block 91) may include any suitable method or reaction for removing oxygen from the gas stream , oxidized compounds, oxidizing agents, or combinations thereof (collectively referred to herein as “oxygen”). Suitable processes or reactions will be apparent to those skilled in the art upon consideration of the present description. Non-limiting examples of suitable oxygen removal methods include various catalytic reactions, contacting with chemical compounds known to interact with oxygen, filtration, absorption, adsorption, heating, cooling, or combinations thereof.

[0095] According to the embodiments of the invention shown in FIG. 2, processing the gas stream may include directing the gas stream 18 to the oxygen removal device 118. According to the embodiments of the invention shown in FIG. 5, processing the intermediate gas stream may include directing the intermediate gas stream 19 to the oxygen removal device 118.

[0096] According to one or more embodiments of the invention described herein, the oxygen removal device 118 may include a device or installation designed to remove oxygen from the gas stream. Non-limiting examples of a suitable oxygen removal device include various reactors (e.g., a fluidized bed reactor or fixed bed), a filter, or combinations thereof. A suitable oxygen removal device 118 may be configured to reduce, prevent, or eliminate the appearance of compounds and / or elements (e.g., oxygen) that can poison the absorbent solvent from the absorption reactor (e.g., as will be described herein).

[0097] According to some embodiments of the invention shown in FIG. 2, the treatment of the gas stream allows the treated gas stream 26 to be substantially free of oxygen. According to some embodiments of the invention shown in FIG. 5, the processing of the intermediate gas stream allows the treated gas stream 41 to be substantially free of oxygen. As used herein, the term “substantially free of oxygen” refers to a fluid stream containing not more than at least about 5% oxygen, alternatively not more than about 1% oxygen, alternatively not more than about 0.1% oxygen, alternatively not more than about 0.01% oxygen by weight relative to the total mass of the stream.

[0098] According to one or more embodiments of the invention described herein, separating at least one gaseous component from a gas stream and / or treated gas stream, collectively referred to as a gas stream (for example, in block 65, 65ʹ, 75 or 75ʹ ), generally includes any suitable method for selectively separating at least the first chemical component or compound from a stream containing the first chemical component or compound and one or more other chemical components, compounds or etc. According to various embodiments of the invention, the gaseous component, separated from the gas stream, may contain one or more hydrocarbons. Non-limiting examples of such hydrocarbons include alkanes (e.g. ethane, butane, isobutane, hexane, or combinations thereof) and alkenes or olefin monomers (e.g. ethylene, hexane or combinations thereof), or optionally comonomers (e.g. butene-1). According to one embodiment of the invention, the gaseous component, separated from the gas stream, may contain unreacted hydrocarbon monomer, for example ethylene. The gaseous component, separated from the gas stream, may contain unreacted hydrocarbon comonomer, for example propene. According to one embodiment of the invention, the gaseous component, separated from the gas stream, may contain unreacted hydrocarbon monomer (for example, ethylene, alone or in combination with other hydrocarbons, such as ethane, isobutane, hexane, or combinations thereof) or, optionally, a hydrocarbon comonomer (for example, propene, alone or in combination with other hydrocarbons, such as isobutane, hexane, or combinations thereof). According to one embodiment of the invention, the gaseous component, separated from the gas stream, may contain ethylene, alone or in combination with isobutane. According to one embodiment of the invention, the capture of isobutane saves the cost of trapped isobutane and reduces the isobutane content in flare emissions. Non-limiting examples of suitable separation methods include distillation, evaporation, flash evaporation, filtration, sieving through membranes, absorption, adsorption, exclusion separation by molecular weight, size exclusion separation, separation based on polarity, or a combination thereof.

[0099] According to one embodiment of the invention, separating the at least one gaseous component from the gas stream may include distilling the gas stream (for example, gas stream 18 shown in FIG. 1, treated gas stream 26 shown in FIG. 2) into one stage so that it is possible to separate at least one gaseous component from other gaseous components depending on the boiling temperature (s). According to such an embodiment of the invention, separating the at least one gaseous component from the gas stream may include distilling the gas stream to produce a stream of light hydrocarbons containing ethylene, ethane, possibly hydrogen, or a combination thereof. According to such an embodiment of the invention, separating the at least one gaseous component from the gas stream may include capturing hexane, hexene, possibly isobutane, or combinations thereof in the bottoms stream of the rectification. According to a further and / or alternative embodiment, separating at least one gaseous component from the gas stream may include trapping isobutane from the side stream of the distillation column.

[00100] According to an embodiment of the system 100 shown in FIG. 1, distillation column 122 may be configured to separate at least one gaseous component by distillation. The gas stream 18 can be directed to a distillation column 122, and the gas stream 18 may contain non-solid components of the vapor-phase polymerization product stream 12 (e.g., nitrogen, methane, ethylene, ethane, propylene, propane, butane, isobutane, pentane, hexane, hexene- 1, heavier hydrocarbons or combinations thereof). The gas stream 18 may contain hydrogen, which can be removed, for example, in separators installed between two polymerization reactors, or using a hydrogenation catalyst in a polymerization reactor (polymerization reactors). At least one gaseous component may exit distillation column 122 in a light hydrocarbon stream 25 and other gaseous components may exit distillation column 122 in a distillation bottoms stream 23. At least one gaseous component released from distillation column 122 in a light hydrocarbon stream 25 shown in FIG. 1 may contain ethylene and may additionally contain other light gases (e.g., ethylene, ethane, methane, carbon dioxide, nitrogen, hydrogen, or combinations thereof). For example, ethylene may be present in the light hydrocarbon stream 25 in an amount of from about 50% to about 99% by weight relative to the total weight of the light hydrocarbon stream 25, alternatively, from about 60% to about 98%, alternatively, from about 70% to about 95 % Other gaseous components released from the distillation column 122 in the bottoms stream of the rectification 23 may contain propylene, propane, butane, isobutane, pentane, hexane, hexene-1, heavier hydrocarbons, or combinations thereof. According to one embodiment of the invention, the bottoms stream of the rectification 23 may be free of olefins, alternatively, substantially free of olefins, alternatively, substantially free of olefins. For example, olefins may be present in the bottoms stream of rectification 23 in an amount of less than about 1.0% by weight relative to the total weight of the bottoms stream of rectification 23, alternatively, less than about 0.5%, alternatively, less than about 0.1%. According to one embodiment of the invention, the side stream 27 containing isobutane can be separated from the distillation column 122 in the side stream 27.

[00101] According to the embodiments of the invention shown in FIG. 1, the lateral stream 27 or at least a portion of the bottoms stream of the distillation 23 can be reused. Recirculation of the side stream 27 or at least a portion of the bottoms stream of the distillation 23 may include, for example, using a suitable pump or compressor, the side stream 27 or at least a portion of the bottoms stream of the rectification 23 back and / or introducing the side stream 27 or at least a portion of the bottoms distillation residue stream 23 into the PES system 100, for example, for reuse in the polymerization reaction. According to one embodiment of the invention, the side stream 27 or at least a portion of the bottoms stream of the distillation 23 can be combined with various other components (catalysts, co-catalysts, etc.) to form a catalyst suspension that can be introduced into one or more reactors 104 , 106. Not wanting to be bound by theory, since the side stream 27 or at least a portion of the bottoms stream of the distillation 23 may contain an olefin-free isobutane stream (alternatively, essentially no soda olefin-containing as described above), side stream 27, or at least a portion of distillation bottoms stream 23 can be mixed with catalytic components (e.g., catalysts, co-catalysts, etc.) without the risk of unintended polymerization reactions (e.g. polymerization to introducing into one or more reactors). Essentially, the side stream 27, or at least a portion of the bottoms stream of the distillation 23, can serve as a source containing no isobutane olefins for the polymerization reaction. Recycling of the side stream 27 or at least a portion of the bottoms stream of the distillation 23 (containing isobutane, not containing olefins) provides an effective and / or cost-effective means of supplying isobutane used to operate the polymerization reaction. According to an alternative embodiment of the invention, the side stream 27 or at least a portion of the bottoms stream of the rectification 23 can be stored for later use in the polymerization reaction or used in any other suitable process.

[00102] According to one embodiment of the invention, at least a portion of the side stream 27 or at least a portion of the bottoms stream of the distillation 23 can be returned to the distillation column 122. For example, a side stream 27 or at least a portion of the bottoms stream of the distillation 23 can be directed using a reboiler to distillation column 122 for further processing.

[00103] The distillation column 122 may be configured in such a way and / or dimensioned so as to permit separation of a suitable volume of gases (for example, a stream of light hydrocarbons 25 shown in FIG. 1). For example, distillation column 122 may operate at a temperature in the range of from about 50 ° C to about 20 ° C, alternatively from about 40 ° C to about 10 ° C, alternatively from about 30 to about 5 ° C, and a pressure in the range of approximately 101 kPa abs. (14.7 psia) to about 3.65 MPa abs. (529.7 psia), alternatively, from about 108 kPa abs. (15.7 psia) to about 2.40 MPa abs. (348 psia), alternatively, from about 0.59 MPa abs. (85 psia) to about 2.0 MPa abs. (290 psia). The distillation column 122 can be made in such a way and / or be dimensioned so as to allow separation of a suitable volume of the gas stream 18 or the treated gas stream (for example, stream 26 shown in Fig. 2). As one skilled in the art will understand, gas stream 18 (possibly a treated gas stream) may remain and / or remain in distillation column 122 for any suitable amount of time that may be necessary to provide a sufficient degree of separation of the components of gas stream 18 ( possibly treated gas stream). According to one embodiment of the invention, the distillation column 122 can be equipped with at least two outlet openings.

[00104] According to one embodiment of the invention, distillation column 122 may be configured and / or may operate such that each stream selected from the light hydrocarbon stream 25 shown in FIG. 1, possibly of the side stream 27 and the bottoms stream of the distillation 23, may contain the desired proportion, part or subgroup of components of the gas stream 18 (possibly the treated gas stream). For example, as one of ordinary skill in the art will understand using the present description, the location of the inlet or outlet for a particular stream, the performance of the distillation column 122, the composition of the gas stream 18 (possibly the treated gas stream), or combinations thereof can be controlled so that this stream may contain a specific one or more components of the gas stream 18 (possibly a processed gas stream).

[00105] According to an alternative embodiment of the invention, separating the at least one gaseous component from the gas stream may include distilling the gas stream (for example, gas stream 18 or processed gas stream 26) in two stages, which allows at least one gaseous component to be separated from the others gaseous components depending on the boiling temperature (s) in the first separation stage and that allows you to separate at least one more gaseous component from other gaseous Components according to the temperature (s) boil the second stage of separation. According to such an embodiment of the invention, separating the at least one gaseous component from the gas stream in a first separation step may include distilling the gas stream to produce an intermediate hydrocarbon stream containing ethylene, ethane, hydrogen, isobutane, or a combination thereof. According to such an embodiment of the invention, separating the at least one gaseous component from the gas stream may include capturing hexane, possibly hexene, or combinations thereof in the bottoms stream of the distillation distillation column used in the first separation stage. In addition, the separation of at least one gaseous component from the gas stream in the second separation stage may include the distillation of ethylene, ethane, possibly hydrogen, or combinations thereof from an intermediate hydrocarbon stream; capturing hexane, possibly hexene, possibly isobutane or combinations thereof in the bottoms stream of rectification in the second separation stage; and possibly capturing isobutane from the side stream of the distillation column in a second separation step.

[00106] According to an embodiment of the system 200 shown in FIG. 2, distillation columns 126 and 124 may be configured to separate at least one gaseous component from the treated gas stream 26 or gas stream 18. The processed gas stream 26 and gas stream 18 may contain non-solid vapor phase polymerisation product stream 12 (e.g. , nitrogen, methane, ethylene, ethane, propylene, propane, butane, isobutane, pentane, hexane, hexene-1, heavier hydrocarbons or combinations thereof). The treated gas stream 26 and gas stream 18 may contain hydrogen, which can be removed, for example, in separators installed between two polymerization reactors, or using a dehydrogenation catalyst in a polymerization reactor (polymerization reactors). The treated gas stream 26 or gas stream 18 can be distilled to produce an intermediate hydrocarbon stream 29. The non-distilled components in the distillation column 126 can exit the distillation column 126 in the bottoms stream of the distillation 43. The side stream 45 can leave the distillation column 126.

[00107] The intermediate hydrocarbon stream 29 can be characterized as a stream containing, alternatively, containing substantially, alternatively, containing substantially alternatively, consisting of C ₄ or lighter hydrocarbons (eg, butane, isobutane, propane, ethane or methane) and any light gases (e.g. hydrogen or nitrogen). For example, C ₄ and lighter hydrocarbons and gases may be present in the intermediate hydrocarbon stream 29 in an amount from about 80% to about 100% by weight relative to the total weight of the intermediate hydrocarbon stream, alternatively from about 90% to about 99.999999%, alternatively from about 99% to about 99.9999%, alternatively, C ₅ and heavier hydrocarbons may be present in the intermediate hydrocarbon stream 29 in an amount of from 0% to about 20% by weight relative to the total weight of the intermediate hydrocarbon stream, alternatively from about 10% to about 0.000001%, alternatively, from about 1.0% to about 0.0001%. In addition, for example, at least 90% by weight of the treated gas stream 26 or gas stream 18 containing C ₄ and lighter hydrocarbons and gases, alternatively at least 98%, alternatively at least, may be present in the intermediate hydrocarbon stream 29 least 99%.

[00108] According to one embodiment of the invention, the flow bottoms distillation 43 can be described as stream comprising C ₆ and heavier components such as alkanes, i.e. alkanes that are hexane (e.g., heptane and / or other large alkanes). In one embodiment, hydrocarbons other than C ₆ and heavier alkanes may be present in the bottoms stream of rectification 43 in an amount of less than about 15%, alternatively, less than about 10%, alternatively, less than about 5% by weight relative to the total weight distillation bottoms stream 43. According to one embodiment of the invention, distillation bottoms stream 43 can be sent to stages or methods of additional processing or, alternatively, they can be removed, if necessary imosti. According to one embodiment of the invention, the bottoms stream of the rectification 43 can be directed to a flare unit for disposal.

[00109] According to one embodiment of the invention, the side stream 45 can be characterized as a stream containing hexene. For example, hexene may be present in side stream 45 in an amount of from about 20% to about 98% by weight relative to the total weight of side stream 45, alternatively, from about 40% to about 95%, alternatively, from about 50% to about 95%.

[00110] According to one embodiment of the invention, sidestream 45 can be reused. According to the embodiment of the invention shown in FIG. 2, recirculation of the side stream 45 may include directing, for example, using a suitable pump or compressor, the side stream 45 back and / or introducing the side stream 45 into the PES 200, for example, for reuse in the polymerization reaction. Recirculation using a side stream 45 (for example, containing hexene) provides an efficient and / or cost-effective means of supplying hexene used to operate the polymerization reaction process. According to one embodiment of the invention, the hexene contained in the side stream 45 can be used in the polymerization reaction as, for example, a comonomer in the reaction. According to an alternative embodiment of the invention, the side stream 45 can be stored for later use in the polymerization reaction or used in any other suitable process.

[00111] According to one embodiment of the invention, the distillation column 126 can be equipped with one or more inlets and at least two outlets. Distillation column 126 may operate at suitable temperature and pressure, for example, which may be suitable for separating the components of the treated gas stream 26 or gas stream 18. For example, distillation column 126 may operate at a temperature in the range of from about 15 ° C. to about 233 ° C. alternatively from about 20 ° C to about 200 ° C, alternatively from about 20 ° C to about 180 ° C, and / or pressure in the range from about 101 kPa (14.7 psi) to about 3.64 MPa ( 527.9 psi), alternatively, from about 108 kPa (15.7 psi) to p imerno 2.40 MPa (348 psi), alternatively from about 0.59 MPa (85 psi) to about 2.0 MPa (290 psi). The distillation column 126 may be configured in such a way and / or dimensioned so as to permit separation of a suitable volume of gases (e.g., flash gas stream). As will be appreciated by one of ordinary skill in the art when considering the present invention, the treated gas stream 26 or gas stream 18 may remain and / or remain in the distillation column 126 for any suitable amount of time, for example, the amount of time that may be necessary to ensure sufficient separation distillation column components 126.

[00112] According to one embodiment of the invention, the treated gas stream 26 or gas stream 18 can be introduced into the distillation column 126 without a compression step, that is, without compression of the treated gas stream 26 or gas stream 18 after it leaves the separator 108 and before it is introduced into distillation column 126. According to another embodiment of the invention, the treated gas stream 26 or gas stream 18 can be introduced into the distillation column 126 at substantially the same pressure as the outlet pressure of the separator 108 e (e.g., at a pressure of from about 101 kPa abs. (14.7 psia) to about 3.64 MPa abs. (527.9 psia), alternatively, from about 108 kPa abs. (15.7 psia) to about 2 , 40 MPa abs. (348 psia), alternatively, from about 0.59 MPa abs. (85 psia) to about 2.0 MPa abs. (290 psia) at the outlet of the evaporation chamber 130). According to another embodiment of the invention, the treated gas stream 26 or gas stream 18 can be introduced into the distillation column 126 without a significant compression step. According to one embodiment of the invention, the treated gas stream 26 or gas stream 18 can be introduced into the distillation column 126 at a pressure in the range of about 0.17 MPa (25 psi) less than the pressure at which the gas stream 18 exits the separator 108, up to about 0.17 MPa (25 psi) more than the pressure at which the gas stream 18 exited the separator 108, alternatively, from about 0.10 MPa (15 psi) less than the pressure at which the gas stream 18 exited from the separator 108, to about 0.10 MPa (15 psi) more than the pressure at which gas stream 18 exited separator 108, alternatively, from about 35.5 kPa (5 psi) less than the pressure at which gas stream 18 exited separator 108, to about 35.5 kPa (5 psi) more than the pressure at which the gas stream 18 exits the separator 108. According to one embodiment of the invention, the treated gas stream 26 or gas stream 18 can be introduced into the distillation column 126 at a pressure in the range of about 101 kPa abs. (14.7 psia) to about 3.64 MPa abs. (527.8 psia), alternatively, from about 108 kPa abs. (15.7 psia) to about 2.40 MPa abs. (348 psia), from about 0.59 MPa abs. (85 psia) to about 2.0 MPa abs. (290 psia).

[00113] According to one embodiment of the invention, distillation column 126 may be configured and / or operable in such a way that each stream selected from the intermediate hydrocarbon stream 29, distillation bottoms stream 43, and possibly side stream 45 may contain the desired the proportion, part or subgroup of the components of the gas stream 18 or the treated gas stream 26. For example, as will be clear to a person skilled in the art using the present description, the location of the outlet for determining divided flow operating parameters of the distillation column 126, part of the treated gas stream 26 or gas stream 18, or combinations thereof can be adjusted so that the stream may contain a particular one or more components of the treated gas stream 26 or gas stream 18.

[00114] According to an embodiment of the system 200 shown in FIG. 2, the intermediate hydrocarbon stream 29 can be separated in a distillation column 124 to produce a light hydrocarbon stream 25, a bottoms stream of a rectification 33, and possibly a side stream 31. The light hydrocarbon stream 25 may comprise ethylene, ethane, possibly hydrogen, or a combination thereof. The distillation bottoms stream 33 may contain isobutane. Side stream 31 may contain isobutane. Isobutane in distillation bottoms stream 33 may contain other isobutane grades than side stream 31. For example, distillation bottoms stream 33 may contain isobutane, which is substantially free of olefins, and side stream 31 may contain recycled isobutane, which may contain olefins.

[00115] At least one gaseous component may exit distillation column 124 in a light hydrocarbon stream 25 and other gaseous components may exit distillation column 124 in distillation bottoms stream 33. At least one gaseous component leaving distillation column 124 the light hydrocarbon stream 25 shown in FIG. 2 may contain ethylene and may further comprise other light gases (e.g., ethylene, ethane, methane, carbon dioxide, nitrogen, hydrogen, or combinations thereof). For example, ethylene may be present in the light hydrocarbon stream 25 in an amount of from about 50% to about 99% by weight relative to the total weight of the light hydrocarbon stream 25, alternatively, from about 60% to about 98%, alternatively, from about 70% to about 95 %

[00116] Other gaseous components leaving the distillation column 124 in the bottoms stream of rectification 33 may contain propylene, propane, butane, isobutane, pentane, hexane, hexene-1, heavier hydrocarbons, or combinations thereof. According to one embodiment of the invention, the distillation bottoms stream 33 may be free of olefins, alternatively substantially free of olefins, alternatively substantially free of olefins. For example, olefins may be present in the bottoms stream of rectification 33 in an amount of less than about 1.0% by weight relative to the total mass of bottoms stream of rectification 33, alternatively, less than about 0.5%, alternatively, less than about 0.1%. According to one embodiment of the invention, the side stream 31, comprising, alternatively, consisting of isobutane, may exit the distillation column 124 in the side stream 31.

[00117] According to one embodiment of the invention, the side stream 31 or at least a portion of the bottoms stream of the distillation 33 can be reused. Recycling the side stream 31 or at least a portion of the distillation bottoms stream 33 may include, for example, using a suitable pump or side stream compressor 31 or at least a portion of the distillation bottoms stream 33 back and / or introducing a side stream 31 or at least as part of the bottoms stream of distillation distillation 33 into the PES 200 system, for example, for reuse in the polymerization reaction. According to one embodiment of the invention, the side stream 31 or at least part of the bottoms stream of the distillation 33 can be combined with various other components (catalysts, joint catalysts, etc.) to obtain a catalyst suspension that can be introduced into one or more reactors 104 106. Without wishing to be bound by theory, since at least a portion of the bottoms stream of the distillation 33 may not contain olefins and may contain isobutane, the stream of the bottoms of the distillation 33 can be mixed with catalytic components (such as catalysts, co-catalysts, and the like) without the risk of occurrence of unintended polymerization reactions (e.g. polymerisation before introduction into one or more reactors). Essentially, at least a portion of the bottoms distillation residue stream 33 may serve as a source of isobutane-free olefins for the polymerization reaction. Recirculation of the side stream 31 or at least a portion of the bottoms stream of the distillation 33 allows an efficient and / or cost-effective means of supplying isobutane to be used for the operation of the polymerization reaction. According to an alternative embodiment of the invention, the side stream 31 or at least a part of the bottoms stream of the distillation 33 can be stored for later use in the polymerization reaction or used in any other suitable process.

[00118] According to one embodiment of the invention, at least a portion of the sidestream 31 or at least a portion of the distillation bottoms stream 33 can be returned to the distillation column 124. For example, sidestream 31 or at least a portion of the distillation bottoms stream 33 can be directed using a reboiler to distillation column 124 for further processing.

[00119] The distillation column 124 may be configured in such a way and / or dimensioned so as to permit separation of a suitable volume of gases (for example, a stream of light hydrocarbons 25 shown in FIG. 2). For example, distillation column 124 may operate at a temperature in the range of from about 50 ° C to about 20 ° C, alternatively from about 40 ° C to about 10 ° C, alternatively from about 30 to about 5 ° C, and a pressure in the range of approximately 101 kPa abs. (14.7 psia) to about 3.65 MPa abs. (529.7 psia), alternatively, from about 108 kPa abs. (15.7 psia) to about 2.40 MPa abs. (348 psia), alternatively, from about 0.59 MPa abs. (85 psia) to about 2.0 MPa abs. (290 psia). The distillation column 124 may be configured in such a way and / or dimensioned so as to allow separation of a suitable volume of the gas stream 18 or the treated gas stream 26. As one skilled in the art will understand, the processed gas stream 26 or gas stream 18 may remain and / or remain in distillation column 124 for any suitable amount of time that may be necessary to ensure sufficient separation of the components of the treated gas stream 26 or gas stream 18. According to one embodiment of the invention, distillation column 124 may be equipped with at least two outlet openings.

[00120] According to one embodiment of the invention, distillation column 124 may be configured and / or may operate such that each stream selected from the light hydrocarbon stream 25 shown in FIG. 2, and distillation bottoms stream 33, may contain the desired fraction, part or subgroup of components of the treated gas stream 26 or gas stream 18. For example, as one skilled in the art will understand using the present description, the location of the inlet or outlet for a particular stream , the operating parameters of the distillation column 124, the composition of the treated gas stream 26 or gas stream 18, or combinations thereof can be adjusted so that this stream may contain a specific one whether more components of the treated gas stream 26 or gas stream 18.

[00121] According to an alternative and / or additional embodiment, separating the at least one gaseous component from the gas stream may include bringing the gas stream into contact with an absorbent (eg, an absorbent solvent system described herein), for example, to allow absorption gaseous component absorbent. According to such an embodiment of the invention, separating the at least one gaseous component from the gas stream includes selectively absorbing the at least one gaseous component from the gas stream. According to such an embodiment of the invention, the absorption of at least one gaseous component from the gas stream as a whole involves bringing the gas stream into contact with a suitable absorbent material, which allows the absorbent to absorb at least one component, and possibly removing an exhaust stream containing non-absorbed gases. According to a further embodiment of the invention, separating the at least one gaseous component from the gas stream may further include separating the absorbed gaseous component from the absorbent.

[00122] According to one embodiment of the invention, bringing the gas stream into contact with the absorbent may include any suitable means of ensuring sufficient contact between the gas stream and the absorbent. Non-limiting examples of suitable methods by which sufficient contact between the gas stream and the absorbent can be ensured include the use of various reactor systems, such as those described above (for example, an absorption column or a bubbler or mixing tank). Without wishing to be limited by theory, a suitable reactor system can provide contact between two or more gaseous, liquid, and / or solid compositions by shaking or mixing the two components in the presence of each other, circulating, dispersing, or diffusing the first composition through the second composition or into the second composition or with using various other methods known to those skilled in the art. According to one embodiment of the invention, the gas stream and the absorbent can be brought into contact in a suitable ratio. This suitable ratio of gas flow to absorbent can range from about 454 kg / h: 3785 l / min (1000 lb / hr: 1000 gpm) to about 1134 kg / h: 95 l / min (2500 lb / hr: 25 gpm) alternatively, from about 454 kg / h: 946 l / min (1000 lb / hr: 250 gpm) to about 1134 kg / h: 379 l / min (2500 lb / hr: 100 gpm), alternatively, about 837 kg / h : 946 l / min (1875 lb / hr: 250 gpm).

[00123] According to one embodiment of the invention shown in FIG. 1-5, separating at least one gaseous component from the gas stream (e.g., gas stream 18 shown in Fig. 1, or treated gas stream 26, shown in Fig. 2, or intermediate gas stream 19, shown in Fig. 3 -5) may include directing the gas stream to the absorption reactor 116. According to one or more embodiments of the invention described herein, the absorption reactor 116 may be a reactor configured to selectively absorb at least a first chemical component or compound from a stream containing a first chemical component or compound and one or more other chemical components, compounds or the like. Non-limiting examples of suitable absorption reactors and / or absorption reactor configurations include an absorption (distillation) tower, a differential pressure absorption (APD) configuration, an irrigation tank, a stirred reactor, one or more compressors, one or more recirculation pumps, or combinations thereof.

[00124] According to one embodiment of the invention, the absorption reactor may be configured to disperse gas in a liquid (for example, by sparging gas through a liquid). For example, according to one embodiment of the invention, the absorption reactor 116 may include a solvent circulation system configured to circulate the solvent through the absorption reactor 116. The flow rate of the solvent circulation can be set depending on the operating conditions of the absorption system described herein below. According to one embodiment of the invention, the absorption reactor 116 may comprise and / or fluidly communicate with one or more pumps configured to recycle the solvent through and / or within the absorption reactor 116. According to a further and / or alternative embodiment, the absorption reactor 116 may comprise a packing layer or column configured to provide small bubble sizes (e.g., gas scattered in the liquid), for example, to provide a relatively large contact surface area between the gas and the liquid, e.g. , to maintain the efficiency of mass transfer and / or absorption of gas by a liquid. According to one embodiment of the invention, the packing of the packing or column layer may comprise a polymeric material, a material with metallic properties, or combinations thereof. According to one embodiment of the invention, the absorption reactor 116 may comprise several layers of packing or columns. In one embodiment, only one section of the absorption reactor 116 may comprise packing material. According to one embodiment of the invention, the material of the packing of the absorption reactor 116 may have random packaging or have a structured packaging. An example of a suitable absorption reactor is given in the Gas Processors Association, ((Engineering Data Book, 10th edition, FIGS. 19-16.

[00125] According to one embodiment of the invention, wherein the absorption reactor 116 is a solvent reactor, the absorption reactor may comprise a suitable system of absorbent solvents, as will be described herein. Such an absorption reactor 116 may be configured to retain an absorbent solvent system. For example, an absorbent solvent system can be stored in the reactor as a liquid, as a fixed bed, or as a fluidized bed.

[00126] According to one embodiment of the invention, a suitable absorbent solvent system may be capable of reversible complexation with ethylene and / or isobutane. Such an absorbent solvent system may generally comprise a complexing agent and a solvent. According to one embodiment of the invention, the system of absorbent solvents can be characterized as a system in which ethylene has selectivity to ethylene compared to ethane, if ethylene and ethane are present at the same partial pressure of about 96.5 kPa (14 psi) at about 40: 1, about 0.14 MPa (20 psi) at about 12: 1, about 0.28 MPa (40 psi) at about 6: 1, and about 1.24 MPa (180 psi) at about 3: 1. According to one embodiment of the invention, said solvent system can be further characterized as having high resistance to pollutants and as exhibiting high stability at elevated and / or varying temperatures and / or pressures or combinations thereof.

[00127] According to one embodiment of the invention, the complex agent may comprise a metal salt. According to such an embodiment of the invention, the metal salt may comprise a salt of one or more transition metals and a weakly ionic halogen. Non-limiting examples of suitable transition metals include silver, gold, copper, platinum, palladium or nickel. Non-limiting examples of suitable weakly ionic halogens include chlorine and bromine. According to one embodiment of the invention, a distinctive feature of a suitable transition metal salt is its high specificity for olefins. Non-limiting examples of suitable halogen transition metal salts include silver chloride (AgCl) and copper chloride (CuCl). According to a particular embodiment of the invention, the salt used in the absorbent solvent system is CuCl. Not wanting to be bound by theory, such a metal salt can interact with the double carbon bonds of olefins (e.g., ethylene).

[00128] According to one embodiment of the invention, the complexing agent may comprise copper (I) carboxylate. According to such an embodiment of the invention, suitable copper (I) carboxylates may be salts of copper (I) and mono-, di- and / or tricarboxylic acids containing from 1 to 20 carbon atoms. The carboxylic acid component of said salt may comprise an aliphatic moiety, a cyclic moiety, an aryl moiety, or combinations thereof. Other suitable examples of copper (I) carboxylates include Cu (I) formate, Cu (I) acetate, Cu (I) propionate, Cu (I) butyrate, Cu (I) pentanoate, Cu (I) hexanoate, Cu (I) octanoate , Cu (I) decanoate, Cu (I) 2-ethyl-hexoate, Cu (I) hexadecanoate, Cu (I) tetradecanoate, Cu (I) methyl formate, Cu (I) ethyl acetate, Cu (I) n-propyl acetate, n Cu (I) butyl acetate, Cu (I) ethyl propanoate, Cu (I) octoate, Cu (I) benzoate, Cu (I) para-tert-butyl benzoate, and the like. According to a further embodiment of the invention, the complexing agent may comprise an addition product of copper (I) carboxylate, for example, as described herein, and boron trifluoride (BF ₃ ).

[00129] According to a further and / or alternative embodiment of the invention, the complexing agent may comprise copper (I) sulfonate. Non-limiting examples of suitable copper (I) sulfonates include salts of copper (I) and sulfonic acids containing from 4 to 22 carbon atoms. The sulfonic acid component of said salt may comprise an aliphatic component, a cyclic component, an aryl component, or combinations thereof. Aliphatic sulfonic acids can be linear or branched. Examples of suitable aliphatic sulfonic acids include, but are not limited to, n-butanesulfonic acid, 2-ethyl-1-hexanesulfonic acid, 2-methylnonansulfonic acid, dodecanesulfonic acid, 2-ethyl-5-n-pentyltridecanesulfonic acid, n-eicosans and etc. Examples of suitable aromatic sulfonic acids include benzenesulfonic acid, alkylbenzenesulfonic acids in which the alkyl moiety contains from 1 to 16 carbon atoms, such as para-toluenesulfonic acid, dodecylbenzenesulfonic acid (ortho-, meta- and para-), para-hexadecylbenzenesulfonic acid ., naphthalenesulfonic acid, phenolsulfonic acid, naphtholsulfonic acids and halobenzenesulfonic acids such as para-chlorobenzenesulfonic acid, para-bromobenzenesulfonic acid and the like.

[00130] According to one embodiment of the invention, the complexing agent may further comprise a hindered olefin. For example, the complexing agent may contain such a hindered olefin according to one embodiment of the invention in which the complexing agent forms a copper complex with insufficient solubility. An example of such a hindered olefin is a propylene tetramer (i.e., dodecene). Not wanting to be bound by theory, a hindered olefin can increase the solubility of the copper complex, as it is easily displaced by ethylene.

[00131] According to various embodiments of the invention, the complexing agent may contain one or more complexing agents described in US patent No. 5104570; 5,191,153; 5,259,986; and 5523512, each of which is incorporated herein by reference in its entirety.

[00132] According to one embodiment of the invention, the solvent may comprise an amine or amine complex, an aromatic hydrocarbon, an olefin, or combinations thereof. Non-limiting examples of solvent amines include pyridine, benzylamine, and aniline. For example, the amine may be aniline (phenylamine, aminobenzene); alternatively, aniline combined with dimethylformamide (DMF), and according to embodiments of the invention, aniline and N-methylpyrrolidone (NMP). According to one embodiment of the invention, in which the solvent contains an aromatic hydrocarbon, said aromatic hydrocarbon may contain unsubstituted or alkyl substituted aryl groups. According to such an embodiment of the invention, under normal environmental conditions, the aromatic hydrocarbon may be in the liquid phase. Suitable non-limiting examples include toluene, xylene, and the like. According to embodiments of the invention in which the solvent contains an olefin, non-limiting examples include olefins containing from 10 to 16 carbon atoms. For example, the olefin may be propylene tetramer, dodecene, tetradecene, hexadecene, or combinations thereof.

[00133] According to one embodiment of the invention, the solvent can be characterized as aprotic, that is, as not containing a dissociable hydrogen atom. Not wishing to be bound by theory, a solvent containing dissociable hydrogen can lead to hydrogenation of a double bond between carbon atoms in an olefin such as ethylene. In addition, the solvent can be characterized as polar, as having a small polarity or as having a unidirectional, electric charge. Not wanting to be bound by theory, a polar solvent can interact with the salt and at least partially solubilize it.

[00134] According to one embodiment of the invention, the solvent can be characterized as a liquid obtained industrially in relatively large volumes, having a relatively low cost, easily transported, or having combinations of these properties. The solvent can be further characterized as having the ability to retain an olefin-metal salt complex or to retain a weakly ionic metal salt, despite fluctuations in temperature and / or pressure.

[00135] According to one embodiment of the invention, the absorbent solvent system may comprise copper chloride, aniline and dimethylformamide (CuCl / aniline / DMF). In an alternative embodiment, the absorbent solvent system may comprise copper chloride, aniline and N-methylpyrrolidone (CuCl / aniline / NMP). According to such an embodiment of the invention, a distinctive feature of the CuO / aniline / NMP solvent system is the increased stability of volatiles at lower pressures and higher temperatures. In alternative embodiments, the absorbent solvent system may comprise copper (I) carboxylate and an aromatic solvent such as toluene or xylene. In alternative embodiments, the absorbent solvent system may comprise copper (I) sulfonate and an aromatic solvent such as toluene or xylene. According to alternative embodiments of the invention, the absorbent solvent system may comprise the product of the addition of copper (I) carboxylate and BF ₃ in an aromatic solvent such as toluene or xylene.

[00136] According to one embodiment of the invention, the absorbent solvent system may comprise copper (I) 2-ethylhexanoate and a propylene tetramer. In one embodiment, the absorbent solvent system may comprise copper (I) 2-ethyl-hexanoate and dodecene. In one embodiment, the absorbent solvent system may comprise copper (I) hexadecanoate and hexadecene. In one embodiment, the absorbent solvent system may comprise copper (I) tetradecanoate and tetradecene.

[00137] According to one embodiment of the invention, the ability of the at least one component to be absorbed by the absorbent may include the ability of the at least one component to reversibly bind, combine, form chemical bonds or combine both with the absorbent or part thereof, for example, by forming various bonds, compounds, affinity, complexes, or combinations thereof. For example, according to one embodiment of the invention in which the absorbent is an absorbent solvent system (for example, a CuCl / aniline / DMF solvent system or a CuCl / aniline / NMP solvent system), the ability to absorb at least one component may include the possibility of complexing between an absorbent and at least one component called an absorbed complex of a particular component (for example, an absorbed ethylene complex).

[00138] The ability to absorb at least one component may further include providing and / or maintaining a suitable ambient pressure in which the gas stream and absorbent are brought into contact, providing and / or maintaining a suitable partial gas pressure, providing and / or maintaining a suitable temperature in an environment in which the gas stream and absorbent are brought into contact, absorption catalytic, or combinations thereof. Without wishing to be bound by theory, the absorption of at least one component with an absorbent can be improved at a suitable temperature and / or pressure.

[00139] According to one embodiment of the invention, the absorption reactor 116 is configured to selectively induce vibrations, changes or cyclical changes in temperature and / or pressure. In one embodiment, the absorption reactor 116 may be configured to selectively absorb and / or induce absorption of unreacted ethylene monomer (and possibly comonomer) from a composition containing various other gases (e.g., ethane, possibly hydrogen). According to another embodiment of the invention, the absorption reactor 116 may be configured to selectively absorb and / or induce absorption of butane, in particular isobutane, from a composition containing various other gases. In yet another embodiment, the absorption reactor 116 may be configured to selectively absorb both unreacted ethylene and butane, in particular isobutane, from a composition containing various other gases (e.g., ethane, possibly hydrogen).

[00140] According to one embodiment of the invention, the absorption reactor 116 may be configured to provide or maintain a suitable temperature, for example, which may depend on the phase in which the absorption reactor is operating at a given time. For example, the absorption reactor 116 may be configured to provide or maintain a suitable temperature, for example, for the purpose of increasing the absorption of the desired chemical compounds, reducing the absorption of the required chemical compounds, instantly evaporating unabsorbed gas from the reactor 116, extracting unreacted ethylene from the absorption reactor 116, and regenerating the absorbent in an absorption reactor 116 or combinations thereof. In one embodiment of the invention, such a suitable temperature may be from about 4.4 ° C (40 ° F) to about 43 ° C (110 ° F), alternatively from about 4.4 ° C (40 ° F) to about 16 ° C (60 ° F), alternatively, from about 4.2 ° C (45 ° F) to about 13 ° C (55 ° F), alternatively, from about 10 ° C (50 ° F) to about 13 ° C (55 ° F), alternatively, about 10 ° C (50 ° F). For example, it was found that the operating temperature of the absorption reactor 116 (and absorbent solvent systems) in the range of from about 4.4 ° C (40 ° F) to about 43 ° C (110 ° F), alternatively, from about 4.4 ° C (40 ° F) to about 16 ° C (60 ° F), alternatively, about 10 ° C (50 ° F) can lead to an unexpected increase in ethylene absorption relative to ethane absorption. Not wanting to be bound by theory, a person skilled in the art will expect (for example, based on the concept of partial pressure in Raoult's law) that the solubility of ethylene and ethane in an absorbing solvent increases with decreasing temperature. However, contrary to these expectations, it was found that the amount of ethylene absorbed in the absorbent solvent and / or the system of absorbent solvents according to the described embodiments of the invention decreases with decreasing temperature below 10 ° C (50 ° F). Due to this unexpected phenomenon, ethylene absorption may be greatest for temperatures ranging from about 4.4 ° C (40 ° F) to about 43 ° C (110 ° F), alternatively, in the range from about 4.4 ° C (40 ° F) to about 16 ° C (60 ° F), alternatively, at a temperature of about 10 ° C (50 ° F). FIG. 11 is a graph showing the solubility with temperature of ethylene and ethane in an absorbent solvent system containing copper chloride, aniline, NMP. The graph illustrates the curve for the expected solubility of ethane and the unexpected trend in the solubility of ethylene over the temperature range above.

[00141] According to one embodiment of the invention, the absorption reactor 116 may be configured to provide or maintain a suitable temperature in the range of from about 4.4 ° C (40 ° F) to about 43 ° C (110 ° F) during the absorption of one or more components of the gas stream (for example, ethylene and / or isobutane). As described above, it was found that the solubility of ethylene unexpectedly turned out to be maximum at temperatures ranging from about 4.4 ° C (40 ° F) to about 16 ° C (60 ° F). In one embodiment, when absorbing ethylene and / or isobutene from the gas stream, absorption reactor 116 may operate at a temperature of from about 4.4 ° C (40 ° F) to about 16 ° C (60 ° F), alternatively, at a temperature approximately 10 ° C (50 ° F). According to an alternative embodiment, when absorbing ethylene and / or isobutene from the gas stream, the absorption reactor may operate at a temperature of from about 16 ° C (60 ° F) to about 43 ° C (110 ° F) or from about 21 ° C (70 ° F) to about 32 ° C (90 ° F). For example, the indicated absorption temperatures of the absorption reactor 116 may be suitable as an economic alternative to operating at a lower temperature (which may require energy consumption during cooling, for example). For example, operating an absorption reactor, such as absorption reactor 116, at temperatures ranging from about 16 ° C (60 ° F) to about 43 ° C (110 ° F) or from about 21 ° C (70 ° F) to about 32 ° C (90 ° F) may require less energy, which saves on production costs due to the ability of the absorption reactor to operate at ambient temperature in a given geographic region.

[00142] According to one embodiment of the invention, the absorption reactor 116 may be configured to provide or maintain a suitable pressure during operation. Such a suitable pressure may be from about 34 kPa gage. (5 psig) to about 3.45 MPa gage. (500 psig), alternatively, from about 0.34 MPa gage. (50 psig) to about 3.10 MPa gage. (450 psig), alternatively, from about 0.52 MPa gage. (75 psig) to about 2.73 MPa gage. (400 psig). According to a further embodiment of the invention, the absorption reactor 116 may be configured to provide or maintain a suitable ethylene partial pressure during operation. Such a suitable ethylene partial pressure may be from about 6.89 kPa abs. (1 psia) to about 2.76 kPa abs. (400 psia), alternatively, from about 207 kPa abs. (30 psia) to about 1.38 MPa abs. (200 psia), alternatively, from about 276 kPa abs. (40 psia) to about 1.72 MPa abs. (250 psia), alternatively, from about 276 kPa abs. (40 psia) to about 0.52 MPa abs. (75 psia), alternatively, from about 276 kPa gage. (40 psig) to about 414 kPa (60 psig), alternatively, approx. 276 kPa huts (40 psig), alternatively, about 414 kPa gage. (60 psig). Not wishing to be bound by theory, increasing the pressure in the absorption reactor 116 may contribute to the absorption of ethylene and / or the formation of a complex of ethylene and a system of absorbent solvents (e.g., CuCl / aniline / NMP systems). In addition, not wanting to be bound by theory, the selectivity of the system of absorbent solvents for ethylene may increase with decreasing pressure of the absorption reactor.

[00143] According to one embodiment of the invention, the absorption reactor 116 may be configured to perform batch and / or continuous processes. For example, according to one embodiment of the invention, the PES system may comprise two or more absorption reactors (for example, such as absorption reactor 116), each of which may be configured to operate in a batch mode. For example, when using two or more absorption reactors, such a system can be configured to operate continuously by absorbing the gas stream component by a “first batch” in the first absorption reactor, while a “second batch” is obtained for absorption in the second absorption reactor. Essentially, by circulating between two or more suitable reactors, the system can operate continuously.

[00144] For example, according to one embodiment of the invention, two or more absorption reactors (eg, an absorption reactor system) may be capable of adsorption with a differential pressure (APD) of ethylene using a liquid solvent, for example, an absorbent solvent system or an absorbent solvent described in this application. According to such an embodiment of the invention, the absorption reactor 116 may comprise two or more absorption reactors configured for APD (for example, an absorption reactor system). In FIG. 10 shows a system of absorption reactors 1000 with four absorption reactors 1010, 1020, 1030, and 1040 configured for ADF. Although the embodiment of the invention shown in FIG. 10 shows four absorption reactors (e.g., absorption reactors 1010, 1020, 1030, and 1040), one of ordinary skill in the art, after considering the present invention, will recognize that two, three, five, six, seven, eight or more absorption can be used in this manner. reactors. According to such an embodiment of the invention, each of the absorption reactors can be made essentially as described in this application. According to one embodiment of the invention, one or more reactors 1010, 1020, 1030, and 1040 may be coupled using a circulation system (for example, containing one or more pumps, valves, pipelines, etc.) to circulate a liquid solvent in reactors 1010, 1020, 1030 and 1040 in the absorption process. Absorption reactors 1010, 1020, 1030 and 1040 can operate in a cyclic mode between the absorption phase (in which a gaseous component, such as ethylene and / or isobutane, is absorbed by the absorbing solvent and / or the system of absorbing solvents) and the regeneration phase (in which the absorbed and / or the gaseous component included in the complex is separated from the system of absorbent solvents and / or the system of absorbent solvents is prepared for reuse, as will be described in this application). For example, reactors 1010, 1020, 1030 and 1040 can operate in a cyclic mode between the absorption and regeneration phases (for example, by means of one or more intermediate phases) in a coordinated mode, so that not all reactors 1010, 1020, 1030, 1040 absorb or regeneration at the same time. According to one embodiment of the invention, in which the absorption reactors 1010, 1020, 1030 and 1040 are configured to operate in the ADF, the reactors 1010, 1020, 1030 and 1040 serve both as absorbers and as regenerators. According to such an embodiment of the invention, separate regeneration tanks may not be required (for example, as described in this application).

[00145] As an example of the operation of the ADF in a consistent mode on a given phase during such operation, the reactor 1010 may act on the absorption phase, for example, under the absorption conditions described in this application. Essentially at the same time, an intermediate pressure can be pumped into the reactor 1020, for example, below the absorption pressure. Furthermore, at substantially the same time, pressure from the intermediate pressure to the regeneration pressure can be reduced in the reactor 1030, while the pressure from the absorption pressure (which was previously in the absorption phase) to the intermediate pressure can be reduced in the reactor 1040. Not wanting to be bound by theory, a decrease in pressure (for example, from absorption pressure to intermediate pressure and from intermediate pressure to regeneration pressure) in each reactor 1010, 1020, 1030 and / or 1040 after absorption can lead to the release of absorbed gaseous components (e.g. ethylene and / or isobutane) from the absorbent and / or regeneration of the absorbent (for example, prepared for reuse, as described in this application). In one embodiment, the pressure of one or more reactors (e.g., reactors 1010, 1020, 1030 and / or 1040) can be used to increase the pressure in the other of these reactors. For example, according to the embodiment of the invention shown in FIG. 10, the gas pressure in reactor 1040 can be used to increase the pressure in reactor 1020 to an intermediate pressure through line 1050 using valves 1058 and 1084 in the open position and valves 1082 and 1056 in the closed position. Valves 1062, 1064, 1066, and 1068 can be switched between open position and closed position, which allows nitrogen in stream 1060 to enter and exit reactors 1010, 1020, 1030, and 1040. Valves 1052, 1054, 1056, and 1058 can be switched between open position and closed position, which allows you to increase and decrease the pressure in the reactors 1010, 1020, 1030 and 1040 using the flow 1050. Valves 1082, 1084, 1086 and 1088 can be switched between the open position and the closed position, which allows the flow of light gases 1080 in reactors 1010 , 1020, 1030 and 1040 in the absorption phase. Valves 1092, 1094, 1096, and 1098 can be switched between the open position and the closed position to remove any purge gas from reactors 1010, 1020, 1030, and 1040 through stream 1090.

[00146] According to one embodiment of the invention, stripping gas, such as isobutane or nitrogen, can be added during the regeneration phase to absorption reactors 1010, 1020, 1030 and 1040, for example, via stream 1070. Stream 1070 can be introduced at the bottom of reactors 1010 , 1020, 1030 and 1040, so that the stripping gas can sparge through the reactor 1010, 1020, 1030 or 1040 (and through any packing materials described in this application). Valves 1072, 1074, 1076, and 1078 can be switched between open and closed positions to add stripping gas to reactors 1010, 1020, 1030, and 1040 during the regeneration process. Not wanting to be bound by theory, stripping gas can lower the partial pressure of ethylene in absorption reactors 1010, 1020, 1030, and 1040 during regeneration.

[00147] According to one embodiment of the invention, one or more absorption reactors 1010, 1020, 1030, and 1040 may include internal elements to distribute the gas through the liquid absorbent solvent and prevent the formation of channels. Suitable internal elements may include a distillation nozzle that distributes gas and reduces longitudinal mixing of the liquid. The internal elements can prevent mixing of the liquid absorbent solvent in the absorption reactors 1010, 1020, 1030 and 1040, so that the solvent stream will saturate first, and then the saturated front can move vertically upward through the absorption reactors 1010, 1020, 1030 and 1040.

[00148] According to one embodiment of the invention, separating the at least one gaseous component from the gas stream includes removing the waste stream. According to one embodiment of the invention, the flow components representing the remaining unabsorbed gas form an exhaust stream. According to one embodiment of the invention, in which the absorbed component contains ethylene and the absorbent contains a solvent system CuCl / aniline / DMF or CuCl / aniline / NMP, said waste stream may contain hydrogen, methane, ethane, acetylene, propylene, various other hydrocarbons, volatile pollutants or combinations thereof. In addition, such a waste stream may essentially not contain unreacted ethylene monomers or, possibly, comonomers. As used herein, the term “substantially free of unreacted ethylene monomers” means that the exhaust gases contain less than 50% of unreacted ethylene monomers, alternatively, less than 10% of unreacted ethylene monomers, alternatively, less than 1.0% of unreacted ethylene monomers, alternatively, less than 0.1 unreacted ethylene monomers, alternatively, less than 0.01% of unreacted ethylene monomers by weight relative to the total mass of the stream.

[00149] According to one embodiment of the invention, removal of the waste stream may include cooling the waste stream and / or lowering or increasing the pressure of the waste stream so that said waste stream enters the processing device 114. For example, according to one embodiment of the invention, the waste stream may be swept away by passing a suitable purge gas (for example, an inert or non-reactive gas, as described above) through a reservoir containing culated gas (e.g., an absorption reactor 116) at a sufficient pressure, with sufficient speed or a combination thereof to displace the exhaust gases. For example, according to some embodiments of the invention shown in FIG. 1-5, separating at least one gaseous component from the gas stream allows to obtain an exhaust gas stream 20 substantially free of unreacted ethylene monomers (possibly comonomers), alternatively, an exhaust gas stream containing a reduced concentration of unreacted ethylene monomers (possibly comonomers ) For example, the exhaust gas stream may contain unreacted ethylene monomers in an amount of less than about 30%, alternatively, less than about 25%, alternatively, less than about 20%, alternatively, less than about 15%, alternatively, less than about 10% by weight relative to the total weight of the stream . According to a further embodiment of the invention, the ethylene content can be reduced in percentage terms relative to the ethylene present in the gas stream until at least one gaseous component is separated from it. For example, the exhaust gas stream may contain unreacted ethylene monomers present in the gas stream prior to separation in an amount of less than about 40%, alternatively, less than about 30%, alternatively, less than about 20% by weight relative to the total weight of the stream.

[00150] According to one embodiment of the invention, separating the at least one gaseous component from the gas stream may further include releasing the absorbed gaseous component from the absorbent (for example, in situ in an absorption reactor 116 and / or in another vessel, such as a regenerator 120). The release of the absorbed gaseous component from the absorbent as a whole includes any suitable means of handling various bonds, compounds, affinities, complexes or combinations thereof, through which at least one gaseous component forms a compound, bond, or combinations thereof with the absorbent or part thereof. Non-limiting examples of suitable methods by which the absorption of the absorbed gaseous component is released include changing the kinetics of absorption or the equilibrium of the absorbent upon absorption, heating or decreasing the pressure of the absorbent, changing the partial pressure of the absorbed gas, or combinations thereof.

[00151] According to one embodiment of the invention, the absorbed gaseous component can be released (for example, by desorption and / or destruction of the complex) from the absorbent within one or more of these absorption reactors in the regeneration and / or desorption phase. According to embodiments of the invention, the regeneration phase may include regenerating a system of absorbent solvents to produce unreacted ethylene; according to embodiments of the invention, the regeneration phase may include regenerating the absorbent solvent system in the absorption reactor 116 to produce unreacted ethylene. For example, according to the embodiment of the invention shown in FIG. 1 and 2 (and / or, according to one embodiment of the invention, in which the absorption reactor 116 is configured to configure the ADF, as described in this application with reference to Fig. 10), the absorption reactor 116 may be configured to induce release from the absorbent the solvent of the gas absorbed by the solvent or forming a complex with it (for example, by desorption and / or destruction of the complex of absorbed ethylene and / or complex of ethylene and / or isobutane), as described in detail in this th application. Not wishing to be bound by theory, inducing the release of absorbed or complexing gas may include changing the kinetics of the reaction or gas-solvent equilibrium of the absorbing solvent system, temperature of the absorption reactor 116, pressure of the absorption reactor 116, partial pressure of the absorbed gas, or a combination thereof. According to such an embodiment of the invention, the absorption reactor 116 may comprise control means, heat pipes, electrical wires, compressors, vacuum devices, and the like. or combinations thereof, configured to alter the reaction kinetics, gas-solvent equilibrium, temperature of the absorption reactor 116, pressure of the absorption reactor 116, or combinations thereof.

[00152] For example, in one embodiment, the evolution of the absorbed gaseous component may include reducing the pressure of the solution containing the ethylene complex to a suitable partial pressure. According to a further embodiment of the invention, the evolution of the absorbed gaseous component may include heating a solution containing an ethylene complex in an absorption reactor 116 (alternatively, in a regenerator 120, as described herein below) to a suitable temperature. Such a suitable temperature may be from about 43 ° C (110 ° F) to about 93 ° C (200 ° F), alternatively from about 60 ° C (140 ° F) to about 71 ° C (160 ° F), alternatively from about 71 ° C (160 ° F) to about 93 ° C (200 ° F), alternatively from about 82 ° C (180 ° F) to about 93 ° C (200 ° F), which promotes the release of the absorbed compound (e.g. ethylene and / or isobutane) from an absorbent solvent. For example, in a particular embodiment, the absorption reactor 116 (alternatively regenerator 120) may operate at a temperature of from about 71 ° C (160 ° F) to about 93 ° C (200 ° F), alternatively from about 82 ° C (180 ° F) to about 93 ° C (200 ° F) during the release of the absorbed component (e.g., ethylene and / or isobutene) from the absorbent solvent. According to an alternative embodiment of the invention, the absorption reactor 116 (alternatively, regenerator 120) can operate at a temperature of from about 60 ° C (140 ° F) to about 71 ° C (160 ° F) during the release of the absorbed component (e.g. ethylene and / or isobutene) from an absorbent solvent. For example, the indicated emission temperatures may be suitable as an economic alternative. For example, the operation of an absorption reactor, such as absorption reactor 116 (alternatively, a regenerator, such as regenerator 120), at temperatures in the range of from about 60 ° C (140 ° F) to about 71 ° C (160 ° F) during the recovery of the absorbed component may require less energy, which saves on production costs due to the use of heat obtained from other sources (for example, from the coolant of the polymerization reactor, low-pressure flow, heat exchangers installed before generators, heat exchangers in the recirculation pipe for the absorbent, polymerization reactors, heating devices with an evaporation line, flash tanks or the like, or combinations thereof) for heating the absorption reactor and / or regenerator.

[00153] Furthermore, according to such an embodiment of the invention, the absorption reactor 116 may be configured to remove gases (for example, previously absorbed and then released gas, such as ethylene) and / or to facilitate the release of absorbed gas due to pressure drop. The absorption reactor 116 may be configured to provide or maintain a suitable partial pressure. Such a suitable partial pressure may be from about 0.7 kPa gage. (0.1 psig) to about 276 kPa (40 psig), alternatively, from about 34 kPa gage. (5 psig) to about 207 kPa (30 psig), alternatively, from about 34 kPa gage. (5 psig) to about 103 kPa (15 psig). According to one embodiment of the invention, the absorption reactor 116 may be configured to provide or maintain a partial ethylene pressure in the range of about 0 MPa abs. (0 psia) to about 34.45 kPa abs. (5 psia).

[00154] According to an alternative embodiment of the invention, separating the at least one gaseous component from the gas stream may further include removing a solution containing a complex of the absorbed component (eg, a complex of absorbed ethylene) for further processing. According to such an alternative embodiment of the invention, the absorbent complex containing the absorbed gaseous component can be removed from the absorption reactor 116 and sent to the regenerator 120 to separate the absorbed gaseous component and / or regenerate the absorbent complex as a complex stream 28. According to embodiments of the invention, the regenerator 120 can regenerate a system of absorbent solvents to produce unreacted ethylene; according to embodiments of the invention, regenerator 120 may regenerate an absorbent solvent system in regenerator 120 to produce unreacted ethylene.

[00155] According to such an embodiment of the invention, the complex stream 28 may comprise ethylene, ethane and / or isobutane. Ethylene may be present in an amount of from about 0.1% to about 10%, alternatively, from about 0.4% to about 5%, alternatively, from about 0.5% to about 2.5% by weight relative to the total weight of the stream. Ethane may be present in an amount of from about 0.1% to about 1%, alternatively, from about 0.2% to about 0.5% by weight relative to the total weight of the stream. Isobutane may be present in an amount of from about 0.1% to about 1%, alternatively, from about 0.2% to about 0.5% by weight relative to the total weight of the stream.

[00156] According to one or more embodiments of the invention described herein, separating the complex stream into a recycle stream and an absorbent stream (for example, in block 92) involves separating the absorbed gaseous component from the absorbent. As shown above, the release of the absorbed gaseous component from the absorbent as a whole includes any suitable methods for reversing various bonds, compounds, affinity, complexes or combinations thereof, through which at least one gaseous component forms a compound, bond, or combinations thereof with an absorbent or part thereof. Various processes and / or emission parameters of the absorbed gaseous component have been described above with respect to the release inside the absorption reactor.

[00157] According to the embodiment of the invention shown in FIG. 5, separating the complex stream into a recycle stream and the absorbent stream may include directing the complex stream 28 to the regenerator 120. According to one or more embodiments of the invention described herein, the regenerator 120 may comprise a device or installation configured to recover, recycle, recycle and / or purifying the absorbent solvent and / or releasing the absorbed gas. Non-limiting examples of a suitable regenerator include a flash reactor, a pressure reduction reactor, a solvent recovery reactor, or combinations thereof.

[00158] According to one embodiment of the invention, the regenerator 120 may be configured to operate based on a pressure difference. According to such an embodiment of the invention, the regenerator 120 may be configured to provide or maintain a suitable internal pressure. Such a suitable internal pressure may be from about 0 MPa gage. (0 psig) to about 1.03 MPa (150 psig), alternatively, from about 34 kPa gage. (5 psig) to about 207 kPa (30 psig), alternatively, from about 34 kPa gage. (5 psig) to about 103 kPa (15 psig), alternatively, from about 0 MPa gage. (0 psig) to about 69 kPa (10 psig). In one embodiment, the regenerator 120 may be configured to provide or maintain a suitable partial pressure. Such a suitable partial pressure may be from about 0 MPa abs. (0 psia) to about 0.34 MPa abs. (50 psia).

[00159] According to one embodiment of the invention, the regenerator 120 may be configured to operate based on elevated temperature. Such a regenerator 120 may be configured to provide or maintain a suitable temperature. Such a suitable temperature may be from about 43 ° C (110 ° F) to about 93 ° C (200 ° F), alternatively from about 60 ° C (140 ° F) to about 93 ° C (200 ° F), alternatively , from about 60 ° C (140 ° F) to about 71 ° C (160 ° F), alternatively, from about 71 ° C (160 ° F) to about 93 ° C (200 ° F), alternatively, from about 82 ° C (180 ° F) to about 93 ° C (200 ° F), which allows evaporation and / or release of the absorbed compound (e.g., ethylene and / or isobutane) from the absorbent solvent. According to one embodiment of the invention, the regenerator 120 (for example, such as an absorption reactor 116) can be heated to desorb or regenerate a system of absorbent solvents using heat sources including cooling water, low pressure steam, or a combination thereof. Cooling water, low pressure steam, or combinations thereof, may be suitable for heating the regenerator 120 (or absorption reactor 116 as described above) to a temperature of from about 60 ° C (140 ° F) to about 93 ° C (200 ° F).

[00160] According to one embodiment of the invention, the regenerator 120 may be configured to perform batch and / or continuous processes. For example, according to one embodiment of the invention, the PES system may comprise two or more absorption regenerators (for example, such as the regenerators 1220 and 1222 shown in FIG. 12), each of which can be used for batch operation. As shown above, when using two or more absorption reactors, such a system can operate and regenerate the absorbent continuously.

[00161] In one embodiment, separating the complex stream into a recycle stream and an absorbent stream allows a regenerated absorbent stream to be reused in the absorption reaction and a recycle stream containing unreacted monomers (possibly comonomers) that can be reintroduced into PES process or reused in the specified process. For example, according to the embodiment of the invention shown in FIG. 5, dividing the complex stream 28 into a recycle stream and an absorbent stream allows to obtain a recycle stream 22, which, for example, can be re-introduced into the purifier 102, and a regenerated absorbent stream 30, which, for example, can be re-introduced into the absorption reactor 116.

[00162] According to one embodiment of the invention, the release of absorbed gas also provides a recycle stream containing unreacted monomers (possibly comonomers) that can be returned to the separator 108 for compression (for example, using one or more compressors installed near the separator 108) . For example, according to some embodiments of the invention shown in FIG. 1-5, the evolution of absorbed gas makes it possible to obtain a recirculated stream 22, which can be returned to the separator 108, 105. Increasing the pressure of the recirculated stream 22 allows to obtain a stream for re-introduction (not shown), which can be re-introduced into the PES process or reused in the specified process. For example, according to some embodiments of the invention shown in FIG. 1-5, the re-introduction stream can be introduced into the cleaner 102. According to an alternative embodiment of the invention, the recycle stream (such as the recycle stream 22) can be pressurized and / or re-introduced into the PES process without returning to the separator 108, 105. According to one embodiment of the invention, the recycle stream 22 may comprise substantially pure ethylene; alternatively, recycle stream 22 may comprise ethylene and butane, in particular isobutane. According to one embodiment of the invention, the gas stream may comprise nitrogen, ethylene, ethane and / or isobutane. Ethylene may be present in an amount of from about 65% to about 99%, alternatively, from about 70% to about 90%, alternatively, from about 75% to about 85% by weight relative to the total weight of the stream. Ethane may be present in an amount of from about 1% to about 20%, alternatively, from about 5% to about 15%, alternatively, from about 7.5% to about 12.5% by weight relative to the total weight of the stream. Isobutane may be present in an amount of from about 1% to about 20%, alternatively, from about 5% to about 15%, alternatively, from about 7.5% to about 12.5% by weight relative to the total weight of the stream.

[00163] According to one or more embodiments of the invention described herein, burning an exhaust gas stream (for example, in block 66 or 76) may generally include burning or burning one or more gaseous components contained in the exhaust gas stream 20. According to one of the embodiments of the invention, the combustion of the exhaust gas stream 20 may additionally or alternatively include cracking, catalytic cracking, pyrolysis, dehydrogenation, scrubbing, conversion, processing or combinations thereof of an exhaust gas stream 20 or combustion products.

[00164] As described herein, the exhaust gas stream 20 may contain vaporized solvents, unreacted gases, secondary products, pollutants, hydrocarbons, or combinations thereof. According to one embodiment of the invention, the exhaust gas stream 20 may comprise hydrogen, nitrogen, methane, ethylene, ethane, propylene, propane, butane isobutane, heavier hydrocarbons, or combinations thereof. Ethylene may be present in an amount of from about 1% to about 40%, alternatively, from about 2.5% to about 20% by weight relative to the total weight of the stream. Ethane may be present in an amount of from about 5% to about 50%, alternatively, from about 30% to about 40% by weight relative to the total weight of the stream. Isobutane may be present in an amount of from about 1% to about 20%, alternatively, from about 1.5% to about 5%, alternatively, from about 2% to about 3% by weight relative to the total weight of the stream. Nitrogen may be present in an amount of from about 10% to about 80%, alternatively, from about 35% to about 50%, alternatively, from about 40% to about 45% by weight relative to the total weight of the stream.

[00165] According to the embodiments of the invention shown in FIG. 1-5, burning the exhaust gas stream may include directing the exhaust gas stream 20 to the processing device 114. According to one or more embodiments of the invention described herein, the processing device 114 may include a combustion device or installation, such as a flare unit. Non-limiting examples of suitable flare units include a burner, incinerator, and the like. or combinations thereof. The flare unit may accordingly comprise one or more adjustable nozzles, an ignition source, a bypass valve, a pressure relief valve, or a combination thereof. The flare unit can be configured to provide an environment for burning various wastes, for example, atomic gases (e.g., nitrogen, oxygen), oxides (e.g., carbon monoxide, nitrogen or sulfur oxides), various undesirable gaseous products, or combinations thereof. According to one embodiment of the invention, the flare unit may further comprise a device or unit configured to selectively remove one or more of the contaminants before combustion, during and / or after combustion (for example, such that the combustion product is not released into atmosphere).

[00166] According to one or more embodiments of the invention described herein, the processing device 114 may include, for example, a cracking unit, a catalytic cracking unit, a scrubber, a converter, a processing unit, a dehydrogenation device, an oxygen removal device, or their combinations. According to one embodiment of the invention, the processing device 114 may comprise an ethylene cracker. In processing device 114, one or more gaseous components, such as ethane, from the exhaust gas stream 20 can be converted into the desired product, such as ethylene monomer. The desired product formed in processing device 114 can be reused in one or more plants selected, for example, from purifier 102, reactor 104, reactor 106.

[00167] According to other alternative embodiments of the invention, the exhaust gas stream 20 can be used as fuel (for example, for steam production or co-production of electrical and thermal energy) and / or can be used as fuel and / or raw material in a thermal cracking unit to obtain ethylene (for example, to obtain a feed stream 10). According to another alternative embodiment of the invention, the exhaust gas from the exhaust gas stream 20 can be sent from the specified installation to the plant to obtain monomer.

[00168] According to one embodiment of the invention, the implementation of one or more of the described systems (eg, PES systems 100, 200, 300, 400 and / or 500) and / or methods (eg, PES methods 600, 700, 800 and / or 900) allows the extraction of a significant part of ethylene monomers, which otherwise would have been lost due to the operation of these systems or methods, for example, by burning gas on a flare. According to one embodiment of the invention, one or more of the described systems allows the extraction of ethylene monomers that would otherwise be lost in an amount of up to about 75%, alternatively, up to about 85%, alternatively, up to about 90%, alternatively, up to about 95% by weight relative to the total mass of the stream. According to one embodiment of the invention, one or more of the described systems allows the recovery of isobutane, which otherwise would have been lost, in an amount up to about 75%, alternatively, up to about 85%, alternatively, up to about 90%, alternatively, up to about 95% by weight relative to the total mass of the stream. The return to circulation of this part of unreacted ethylene monomers allows to obtain significant economic benefits, for example, by improving the efficiency of using ethylene monomers and reducing capital costs associated with the acquisition of ethylene monomers. Likewise, the return to circulation of this portion of isobutane provides significant economic benefits, for example, by reducing the capital costs associated with the acquisition of isobutane and / or by reducing the presence of isobutane in flare emissions.

[00169] According to one embodiment of the invention, the introduction of one or more of the described systems and / or methods reduces the amount of ethane and / or hydrogen that is sent to the polymerization reactor 106. According to one embodiment of the invention, the implementation of one or more of the described systems and / or methods can reduce the amount of ethane and / or hydrogen that is returned to the polymerization reactor (such as reactors 104 and / or 106) with a recycle stream. By reducing the amount of ethane contained in the stream sent to the polymerization reactor, the overall efficiency of producing polyethylene can be improved (for example, by increasing the concentration of ethylene without reaching the boiling point in the loop reactor). For example, reducing the amount of ethane in the stream can improve the efficiency of the polymerization reactor, improve the efficiency of the catalyst, reduce the clogging of the equipment with the polymer, reduce the downtime during polymerisation, improve the production of bimodal types of polymer, improve the production of copolymers or a combination thereof.

[00170] The various embodiments of the invention shown in the drawings may be simplified and conventional equipment such as heat exchangers, pumps and compressors not shown; however, one skilled in the art will understand that the described processes and systems may include such equipment typically used in all polymer manufacturing sites.

[00171] A person skilled in the art will understand that industrial and commercial methods for producing polyethylene may require the use of one or more, often several, compressors or similar installations. These compressors are used in all areas of polyethylene production, for example, to lower the pressure in reactors 104, 106 during polymerization. In addition, one skilled in the art will understand that the polyethylene production process involves the use of one or more deoxygenation plants and / or similar oxygen removal units, for example, for cleaning solvents or reagents and / or for purging oxygen removal reactors. Since the enterprise for the industrial production of polyethylene already has the infrastructure and means of its maintenance, for example, for supplying power and technical operation of compressors and / or oxygen removal plants, redistributing a part of the indicated available resources for use in the described systems may require small, if any additional capital costs for the implementation of the described systems and or methods.

[00172] In addition, since compressors, oxygen scavengers, and various other components are already used in various processes and systems for producing polyethylene, the ability to operate such plants in enhanced mode can increase the overall efficiency of systems and processes in the production of polyethylene. For example, in the event that part of the PES process or system operates autonomously during maintenance and / or repair, other parts of the system (e.g., compressor, deoxygenation unit, reactor, etc.) may continue to provide service according to these processes. The functioning and / or redistribution of resources for the operation of the described systems and / or PES methods allow, thereby, to increase the efficiency of the use of traditional systems.

ADDITIONAL DESCRIPTION

[00173] Methods and systems for separating components in a polymerizing system have been described. The following claims are provided as additional description:

[00174] An embodiment of the invention A

A method for separating components in a polymer production system, comprising:

separating the stream of polymerization products into a gas stream and a polymer stream, wherein the gas stream contains ethane and unreacted ethylene;

distillation of the gas stream to obtain a stream of light hydrocarbons containing ethane and unreacted ethylene;

bringing the light hydrocarbon stream into contact with the absorbent solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorbent solvent system; and

extracting an exhaust gas stream from an absorbent solvent system, wherein the exhaust gas stream contains ethane, hydrogen, or combinations thereof.

[00175] An embodiment of the invention B

A method according to an embodiment of the invention A, further comprising:

regeneration of an absorbent solvent system to produce recovered ethylene.

[00176] An embodiment of the invention C

A method according to an embodiment of the invention A, further comprising:

distillation of the gas stream to obtain a side stream containing isobutane.

[00177] An embodiment of the invention D

A method according to an embodiment of the invention A, further comprising:

processing the flow of exhaust gases in the processing device.

[00178] An embodiment of the invention E

A method according to an embodiment of the invention D, in which the processing device includes a cracking unit, a catalytic cracking unit, a scrubber, a converter, a processing device, a dehydrogenation device, an oxygen removal device, a flare unit, or combinations thereof.

[00179] An embodiment of the invention F

The method of Embodiment A, wherein the absorbent solvent system is configured to operate at a temperature in the range of about 4.4 ° C (40 ° F) to about 43 ° C (110 ° F).

[00180] An embodiment of the invention G

The method of Embodiment A, wherein the absorbent solvent system comprises copper chloride, aniline and N-methylpyrrolidone.

[00181] An embodiment of the invention H

A method for separating components in a polymer production system, comprising:

separating the stream of polymerization products into a gas stream and a polymer stream, wherein the gas stream contains ethane and unreacted ethylene;

distillation of the gas stream to obtain an intermediate hydrocarbon stream and a first bottoms stream, wherein the intermediate hydrocarbon stream contains ethane, ethylene and isobutane;

distillation of the intermediate hydrocarbon stream to produce a light hydrocarbon stream and a second bottoms stream, wherein the light hydrocarbon stream contains ethane and ethylene;

bringing the light hydrocarbon stream into contact with the absorbent solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorbent solvent system; and

extracting an exhaust gas stream from an absorbent solvent system, wherein the exhaust gas stream contains ethane, hydrogen, or combinations thereof.

[00182] An embodiment of the invention I

A method according to an embodiment of the invention H, further comprising:

regeneration of an absorbent solvent system to produce recovered ethylene.

[00183] An embodiment of the invention J

A method according to an embodiment of the invention H, further comprising:

distillation of the intermediate hydrocarbon stream to obtain a side stream containing isobutane, wherein the second bottoms stream contains isobutane and is substantially free of olefins.

[00184] An embodiment of the invention K

A method for separating components in a polymer production system, comprising:

polymerizing olefin monomers in a first polymerization reactor to produce an intermediate polymerization product stream;

separating the intermediate polymerization product stream into an intermediate gas stream and an intermediate polymer stream, wherein the intermediate gas stream contains ethane, unreacted ethylene and hydrogen; and

polymerization of the intermediate polymer stream in a second polymerization reactor.

[00185] An embodiment of the invention L

The method according to an embodiment of the invention K, a separation step comprising lowering the pressure of the intermediate polymerization product stream to instantly vaporize ethylene, ethane, hydrogen, or combinations thereof.

[00186] An embodiment of the invention M

A method for separating components in a polymer production system, comprising:

polymerizing olefin monomers in a first polymerization reactor;

separating the intermediate polymerization product stream into an intermediate gas stream and an intermediate polymer stream, wherein the intermediate gas stream contains ethane and unreacted ethylene;

polymerization of the intermediate polymer stream in a second polymerization reactor; and

introducing an absorber in front of the second polymerization reactor.

[00187] An embodiment of the invention N

The method according to a variant implementation of the invention M, the introduction of the scavenger in front of the second polymerization reactor, comprising introducing the scavenger into the intermediate polymerization product stream.

[00188] An embodiment of the invention O

The method according to a variant implementation of the invention M, in which the absorber contains a hydrogenation catalyst.

[00189] An embodiment of the invention P

The method according to an embodiment of the invention M, wherein the separation step comprises:

lowering the pressure of the intermediate polymerization product stream for instant evaporation of ethylene and ethane.

[00190] An embodiment of the invention Q

The method according to a variant implementation of the invention M, in which the absorber reduces the concentration of hydrogen in front of the second polymerization reactor.

[00191] An embodiment of the invention R

A method for separating components in a polymer production system, comprising:

polymerizing olefin monomers in a first polymerization reactor to produce an intermediate polymerization product stream;

degassing at least a portion of the hydrogen from the intermediate polymerization product stream to produce a product stream with a reduced hydrogen content;

separating the product stream with a reduced hydrogen content into an intermediate gas stream and an intermediate polymer stream, wherein the intermediate gas stream contains ethane and unreacted ethylene; and

polymerization of the intermediate polymer stream in a second polymerization reactor.

[00192] An embodiment of the invention S

The method according to an embodiment of the invention R, a separation step comprising lowering the pressure of the product stream with a reduced hydrogen content for instant evaporation of ethylene and ethane.

[00193] An embodiment of the invention T

The method according to a variant implementation of the invention R, in which the amount of hydrogen in the intermediate gas stream is less than about 1% of the mass.

[00194] An embodiment of the invention U

A method according to an embodiment of the invention R, further comprising:

bringing the intermediate gas stream into contact with the absorbent solvent system, wherein at least a portion of the unreacted ethylene from the intermediate gas stream is absorbed by the absorbent solvent system; and

regeneration of an absorbent solvent system to produce recovered ethylene.

[00195] An embodiment of the invention V

A method according to an embodiment of the invention R, further comprising:

extracting an exhaust gas stream from an absorbent solvent system, wherein the exhaust gas stream contains ethane.

EXAMPLES

[00196] The present invention has been described generally, the following examples are given as specific embodiments of the invention and demonstrate its practical application and advantages. It should be understood that these examples are provided by way of illustration and are not intended to limit the description or claims in any way.

[00197] An automated installation simulating an industrial process was used to obtain output when applying a model corresponding to the systems and / or methods described in this application. The applicable model is shown in FIG. 12, an embodiment of an absorbent system 1200 described herein is shown and will be used to describe the examples below. According to the embodiment of the invention shown in FIG. 12, a stream of light gases 1218, which was separated from the stream of polymerization products exiting the reactor to produce polyethylene 104, 106 described in an embodiment of the PES systems 100, 200, 300, 400 or 500 shown in FIG. 1-5, fed to the absorption reactor 1216. The total molar and mass flow rates and the molar and mass flow rates of the components of the light gas stream 1218 are shown in table 1 below:

Table 1

[00198] The unreacted ethylene, which enters the absorption reactor 1216, was absorbed in the absorbent solvent system in the absorption reactor 1216. The absorbed unreacted ethylene was transferred as a complex stream 1228 to the first regenerator 1220. In the stream 1228, the absorbed ethylene was heated using a REG 1 HEAT heat exchanger before feeding into the first regenerator 1220. Ethylene was stripped from the solvent from the absorbent solvent system in the first regenerator 1220 and sent via stream 1229 to the second regenerator 1222. otok 1229 can be cooled using a heat exchanger before entering REG2COOL second regenerator 1222. Ethylene was recovered in the flow 1224. The absorption solvent in streams 1232 and 2134 are combined in FEEDCOOL exchanger for reuse in the absorption reactor 1216 in the flow 1230.

[00199] Table 2 shows the operating conditions for examples 1-44 of ethylene recovery using the system 1200 shown in FIG. 12. For the examples shown in table 2, the system of absorbent solvents contained the system based on copper chloride, aniline and NMP, described in this application, and the composition of the purified product based on 90% recovery of ethylene. The composition of the purified product recovered from stream 1224 in FIG. 12 included ethylene, ethane, nitrogen, hydrogen, and isobutane. % of the mass. each of these components in the purified product is shown in table 2. Selected examples from table 2 are discussed in detail below.

EXAMPLE 3

[00200] In Example 3 shown in Table 2, the absorption reactor 1216 shown in FIG. 12, operated at a temperature of -9.4 ° C (15 ° F), while the temperature of the regenerated solvent was -10 ° C (14 ° F) and a pressure of 276 kPa gage. (40 psig). The first regenerator 120 operated at a temperature of 66 ° C (150 ° F) and a pressure of 0 MPa gage. (0 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 MPa gage. (0 psig). Under such conditions, system 900 allows the recovery of 90% ethylene, the flow rate of the solvent circulation is 1563878 kg / h (344776 lb / h) and the amount of ethylene in the purified product is 64.5%.

EXAMPLE 4

[00201] In Example 4, shown in Table 2, the operating conditions are the same as in Example 3, except that the first regenerator 1220 was operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 MPa gage. (0 psig). Under such conditions, system 900 allows the recovery of 90% ethylene at a flow rate of solvent circulation of 65,198 kg / hr (143,736 lb / hr), while the purified product contains 77.5% ethylene.

EXAMPLE 7

[00202] In Example 7 shown in Table 2, the absorption reactor 1216 shown in FIG. 12, operated at a temperature of 12 ° C (53 ° F), while the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 276 kPa gage. (40 psig). The first regenerator 120 operated at a temperature of 66 ° C (150 ° F) and a pressure of 0 MPa gage. (0 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 MPa gage. (0 psig). Under these conditions, system 900 allows the recovery of 90% ethylene at a flow rate of 24,458 kg / h of solvent (53920 lb / h). The composition of the purified product for example 7 is shown in table 2.

[00203] When comparing example 7 with examples 3 and 4, the flow rate of the solvent circulation of 24458 kg / h (53920 lb / h) in example 7 is less than the flow rates of 65198 kg / h (143736 lb in examples 3 and 4) / hour) and 1563878 kg / h (344776 lbs / hour). Thus, Example 7 showed that the flow rate of the solvent circulation required for ethylene absorption in the system of absorbent solvents based on copper chloride, aniline and NMP is much lower at an absorption temperature of 12 ° C (53 ° F) than for an absorption temperature of 9.4 ° C (15 ° F) due to an unexpected drop in the solubility of ethylene in said absorbent solvent system at temperatures below about 10 ° C (50 ° F).

EXAMPLE 8

[00204] In Example 8 shown in Table 2, the absorption reactor 1216 shown in FIG. 12, operated at a temperature of 13 ° C (55 ° F), while the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 276 kPa gage. (40 psig). The first regenerator 1220 operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 MPa gage. (0 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 MPa gage. (0 psig). Under such conditions, system 800 can recover 90% ethylene at a flow rate of solvent circulation of 21,675 kg / h (47,785 lb / h). The composition of the purified product for example 8 is shown in table 2.

[00205] Example 8 confirms the results obtained in example 7 about the need to use a lower solvent circulation flow when the absorption reactor 1216 was operated at a temperature of 13 ° C (55 ° F) rather than at temperatures below 10 ° C (50 ° F). In addition, Example 2 shows that changing the temperature of the regenerator 1220 from 66 ° C (150 ° F) to 93 ° C (200 ° F) does not significantly affect the flow rate of the solvent.

EXAMPLE 19

[00206] In Example 19, shown in Table 2, the absorption reactor 1216 shown in FIG. 12, operated at a temperature of 12 ° C (53 ° F), while the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 276 kPa gage. (40 psig). The first regenerator 1220 was operated at a temperature of 93 ° C (200 ° F) and a pressure of 69 kPa. (10 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 69 kPa gage. (10 psig). Under these conditions, system 1200 allows the recovery of 90% ethylene at a flow rate of solvent circulation of 26885 kg / h (59272 lb / h). The composition of the purified product is shown in table 2.

[00207] Example 19 confirmed the lower solvent circulation rates discussed in Examples 7 and 8 compared to Examples 3 and 4. Example 19 also shows that the pressure changes of the first and second regenerators 1220 and 1222 in the range of 0 MPa gage. (0 psig) up to 69 kPa (10 psig) has no significant effect on the results. The action of regenerators 1220 and 1222 at 0 MPa (0 psig) allows you to provide a lower flow rate of circulation of the solvent, as well as increased purity of the product, and the operation of the regenerators 1220 and 1222 at 69 kPa g. (10 psig) allows for a safe design, since the positive pressure in the regenerators 1220 and 1222 reduces the possibility of air and water leakage due to leaks in the specified system and process, which can interact with copper chloride in the system of absorbent solvents and adversely affect performance.

EXAMPLE 28

[00208] In Example 28, shown in Table 2, the absorption reactor 1216 shown in FIG. 12, operated at 11 ° C (52 ° F), and the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 0.41 MPa gage. (60 psig). The first regenerator 1220 operated at a temperature of 38 ° C (100 ° F) and a pressure of 0 MPa gage. (0 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 MPa gage. (0 psig). Under these conditions, system 1200 allows the recovery of 90% ethylene at a flow rate of solvent circulation of 26,586 (58,613 lb / hr). The composition of the purified product is shown in table 2.

[00209] Under the conditions used in example 28, the flow rate of the solvent circulation is less than the flow rate in examples 3 and 4, while the amount of ethylene in the purified product is much higher.

EXAMPLE 29

[00210] In Example 29 shown in Table 2, the absorption reactor 1216 shown in FIG. 12, operated at 13 ° C (55 ° F), and the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 0.41 MPa gage. (60 psig). The first regenerator 1220 operated at a temperature of 66 ° C (150 ° F) and a pressure of 0 MPa gage. (0 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 MPa gage. (0 psig). Under these conditions, system 1200 allows the recovery of 90% ethylene at a flow rate of solvent circulation of 23181 kg / h (51106 lb / h). The composition of the purified product is shown in table 2.

[00211] Under the conditions used in example 29, the flow rate of the solvent circulation is less than the flow rate in examples 3 and 4, while the amount of ethylene in the purified product is much higher.

EXAMPLE 30

[00212] In Example 30 shown in Table 2, the absorption reactor 1216 shown in FIG. 12, operated at 13 ° C (56 ° F), wherein the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 0.41 MPa gage. (60 psig). The first regenerator 1220 operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 MPa gage. (0 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 MPa gage. (0 psig). Under these conditions, system 1200 allows the recovery of 90% ethylene at a flow rate of the solvent flow of 21,203 kg / h (46,744 lb / h). The composition of the purified product is shown in table 2.

[00213] Under the conditions used in example 30, the flow rate of the solvent circulation is less than the flow rate in examples 3 and 4, while the amount of ethylene in the purified product is much higher.

EXAMPLE 33

[00214] In Example 33 shown in Table 2, the absorption reactor 1216 shown in FIG. 12 operated at a temperature of 39 ° C (102 ° F), while the temperature of the regenerated solvent was 38 ° C (100 ° F). The absorption reactor 1216 also operated at a pressure of 0.41 MPa gage. (60 psig). The first regenerator 1220 operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 MPa gage. (0 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 MPa gage. (0 psig). Under these conditions, system 900 allows the recovery of 90% ethylene at a solvent flow rate of 28,774 kg / h (63,435 lb / h). The composition of the purified product for example 33 is shown in table 2.

[00215] Under the conditions used in example 33, the flow rate of the solvent circulation is less than the flow rate in examples 3 and 4, while the amount of ethylene in the purified product is much higher. In addition, example 33 shows that the action of the absorption reactor 116 at temperatures above the maximum solubility temperatures shown in the solubility graph, for example, at 39 ° C (102 ° F), as shown in example 33, may still be economically feasible, since for example, the flow rate of the solvent circulation remains low compared with the conditions in examples 3 and 4.

EXAMPLE 40

[00216] In Example 40 of Table 2, the absorption reactor 1216 shown in FIG. 12, operated at a temperature of 11 ° C (52 ° F), while the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 0.41 MPa gage. (60 psig). The first regenerator 1220 operated at a temperature of 66 ° C (150 ° F) and a pressure of 69 kPa. (10 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 69 kPa gage. (10 psig). Under these conditions, system 1200 allows 90% of ethylene to be extracted at a solvent flow rate of 26055 kg / h (57441 lb / h). The composition of the purified product for example 40 is shown in table 2.

[00217] Under the conditions used in example 40, the flow rate of the solvent circulation is less than the flow rate in examples 3 and 4, while the amount of ethylene in the purified product is much higher.

EXAMPLE 41

[00218] In Example 41 of Table 2, the absorption reactor 1216 shown in FIG. 12, operated at 13 ° C (55 ° F), and the temperature of the regenerated solvent was 10 ° C (50 ° F). The absorption reactor 1216 also operated at a pressure of 0.41 MPa gage. (60 psig). The first regenerator 1220 was operated at a temperature of 93 ° C (200 ° F) and a pressure of 69 kPa. (10 psig). The second regenerator 1222 operated at a temperature of 10 ° C (50 ° F) and a pressure of 69 kPa gage. (10 psig). Under these conditions, system 900 allows the recovery of 90% ethylene at a flow rate of the solvent flow of 23,352 kg / h (51,482 lb / h). The composition of the purified product is shown in table 2.

[00219] Under the conditions used in example 41, the flow rate of the solvent circulation is less than the flow rate in examples 3 and 4, while the amount of ethylene in the purified product is much higher.

MODELING EXAMPLE

[00220] An automated installation simulating an industrial process was used to obtain the output of a model corresponding to the systems and / or methods described in this application. The applicable model is shown in FIG. 13, in which the gaseous stream designated VAPFEED (for example, the light gas stream described herein) is fed to an ASORB1 absorption reactor. The output generated by a plant simulating an industrial process was the material balance and heat balance shown in Table 3. The names indicating the various streams listed in Table 3 correspond to the streams shown in FIG. 10. In FIG. 13 ASORB1 is an absorption reactor that is shown as a four stage absorber operating at 32 ° C (90 ° F).

[00221] At least one embodiment of the invention is described herein, with variations, combinations, and / or modifications of an embodiment (s) and / or properties of an embodiment (s) made by a person skilled in the art within the scope of the present invention. . Alternative embodiments of the invention that result from combining, combining and / or eliminating the properties of the embodiment of the invention are also within the scope of the present invention. In the case where the numerical ranges or limitations are indicated in a direct form, it should be understood that such precisely defined ranges or limitations include iterative ranges or limitations of a similar value falling within the indicated explicit ranges or limitations (for example, from about 1 to about 10 includes, 2, 3, 4, etc .; more than 0.10 includes 0.11, 0.12, 0.13, etc.). For example, if a numerical range is given with a lower limit, R ₁ , and an upper limit, R _U , any number falling within the indicated range is specifically disclosed. In particular, the following numbers are specifically disclosed within the range: R = R ₁ + k * (R _u -R ₁ ), wherein k is a variable in the range from 1 percent to 100 percent in a 1 percent increment, i.e. k represents 1 percent, 2 percent, 3 percent, 4 percent, 5 percent, ... 50 percent, 51 percent, 52 percent, ... 95 percent, 96 percent, 97 percent, 98 percent, 99 percent or 100 percent. In addition, any numerical range limited by the two R numbers defined above is also specifically disclosed. The use of the term “possible” with respect to any element of the claims means that the element is necessary or, alternatively, the element is not necessary, both alternatives being within the scope of the claims. It should be understood that the use of broader terms, such as contains, includes and has, provides support for narrower terms, such as consisting of, consisting mainly of and containing essentially of. Accordingly, the scope of legal protection is not limited to the description set forth above, but is determined by the claims below, while this scope includes all equivalents of the subject invention according to the claims. Each and all claims is included in the form of a further description in the present application, the claims being an embodiment (s) of the implementation of the described claimed subject matter. The discussion of the link in the present description is not an assumption that the link is a prior art, in particular any link having a publication date after the priority date of this application. A description of all patents, patent applications, and patent publications cited in this application is hereby incorporated by reference to the extent that they provide typical, methodological or other details that complement the present invention.

Claims (34)

1. The method of separation of components in a polymer production system, including: a. separating the stream of polymerization products into a gas stream and a polymer stream, wherein the gas stream contains ethane and unreacted ethylene; b. distillation of the gas stream to obtain a stream of light hydrocarbons containing ethane and unreacted ethylene; c. bringing the light hydrocarbon stream into contact with the absorbent solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorbent solvent system; and d. extracting an exhaust gas stream from an absorbent solvent system, wherein the exhaust gas stream contains ethane, hydrogen, or a combination thereof; e. regeneration of an absorbent solvent system to produce recovered ethylene, moreover, the system of absorbent solvents contains copper chloride, aniline and N-methylpyrrolidone. 2. The method according to p. 1, further comprising: distillation of the gas stream to obtain a side stream containing isobutane. 3. A method of separating components in a polymer production system, including: a. separating the stream of polymerization products into a gas stream and a polymer stream, wherein the gas stream contains ethane and unreacted ethylene; b. distillation of the gas stream to obtain an intermediate hydrocarbon stream and a first bottoms stream, wherein the intermediate hydrocarbon stream contains ethane, ethylene and isobutane; c. distillation of the intermediate hydrocarbon stream to produce a light hydrocarbon stream and a second bottoms stream, wherein the light hydrocarbon stream contains ethane and ethylene; d. bringing the light hydrocarbon stream into contact with the absorbent solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorbent solvent system; and e. extracting an exhaust gas stream from an absorbent solvent system, wherein the exhaust gas stream contains ethane, hydrogen, or a combination thereof; f. regeneration of an absorbent solvent system to produce recovered ethylene, moreover, the system of absorbent solvents contains copper chloride, aniline and N-methylpyrrolidone. 4. The method according to p. 3, further comprising: distillation of the intermediate hydrocarbon stream to produce a side stream containing isobutane, wherein the second bottoms stream contains isobutane, the second bottoms stream being substantially free of olefins. 5. A method for separating components in a polymer production system, including: a. polymerizing olefin monomers in a first polymerization reactor to produce an intermediate polymerization product stream; b. degassing at least a portion of the hydrogen from the intermediate polymerization product stream to produce a product stream with a reduced hydrogen content; c. separating the product stream with a reduced hydrogen content into an intermediate gas stream and an intermediate polymer stream, wherein the intermediate gas stream contains ethane and unreacted ethylene; and d. polymerization of the intermediate polymer stream in a second polymerization reactor; e. bringing the intermediate gas stream into contact with the absorbent solvent system, wherein at least a portion of the unreacted ethylene from the intermediate gas stream is absorbed by the absorbent solvent system; f. extracting an exhaust gas stream from an absorbent solvent system, wherein the exhaust gas stream contains ethane; g. regeneration of an absorbent solvent system to produce recovered ethylene, moreover, the system of absorbent solvents contains copper chloride, aniline and N-methylpyrrolidone 6. The method according to p. 5, characterized in that the separation stage includes lowering the pressure of the product stream with a low hydrogen content for instant evaporation of ethylene and ethane. 7. The method according to p. 5, characterized in that the amount of hydrogen in the intermediate gas stream is less than about 1% of the mass. 8. The method according to p. 5, further comprising: processing the flow of exhaust gases in the processing device. 9. The method according to p. 8, characterized in that the processing device includes a cracking unit, a catalytic cracking unit, a scrubber, a converter, a treatment unit, a dehydrogenation device, an oxygen removal device, a flare unit, or combinations thereof. 10. The method according to p. 9, characterized in that the system of absorbent solvents is configured to operate at a temperature in the range from about 4.4 ° C (40 ° F) to about 43 ° C (110 ° F).

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